Methods and systems for processing a high-concentration protein product from a microcrop and compositions thereof

ABSTRACT

The present disclosure relates, according to some embodiments, to methods and systems for processing a high-concentration protein product from a microcrop (e.g., aquatic species,  Lemna ) and compositions thereof. According to some embodiments, the present disclosure relates to a method of processing a biomass comprising a microcrop (e.g.,  Lemna ), where the method may include: blanching a first portion of the biomass in a blanching solution to form a wet protein concentrate; separating the first wet protein concentrate from a separated solution (e.g., using a screw press, using a vibratory screen); and drying the first wet protein concentrate to form at least one of a first protein concentrate flake and a first protein concentrate granule. In some embodiments at least one of the first protein concentrate flake and the first protein concentrate granule may comprise at least 45% protein and a Protein Digestibility Corrected Amino Acid Score (PDCAAS) value of at least 0.88. In some embodiments, the present disclosure relates to protein products and compositions derived from a microcrop (e.g., derived from  Lemna ).

CROSS-REFERENCE TO RELATED APPLICATIONS

This application claims priority to the provisional filing U.S.Application No. 62/216,975 filed Sep. 10, 2015, the contents of whichare hereby incorporated in their entirety by reference.

FIELD OF THE DISCLOSURE

The present disclosure relates, in some embodiments, to methods andsystems for processing a protein product (e.g., a high-concentrationprotein product) from a microcrop (e.g., aquatic species, Lemna,Wolffia) and compositions thereof.

BACKGROUND OF THE DISCLOSURE

An ever-increasing global population continues to fuel a plethora ofsustainability concerns including sufficient and affordable access toprotein sources for both feed animals and human consumption,particularly in developing nations. While marine protein sources areoften utilized in feeds due to their desirable nutritional profile andenhanced palatability, high production costs lead to an increased demandfor alternatives. However, many plant species are unsuitablealternatives due to qualities such as inferior amino acid profile,inferior protein quality and/or quantity, inferior digestibility, highfiber content, and/or high oxalic acid content. Additionally, waterconservation concerns—particularly in equatorial and arid regions—are adriving factor in identifying suitable alternative species for theproduction of protein concentrates.

SUMMARY

Accordingly, a need has arisen for improved methods and systems for theproduction of a protein product (e.g., a high-concentration proteinproduct). Furthermore, a need has arisen for improved methods andsystems for the production of a protein product (e.g., ahigh-concentration protein product) with reduced oxalic acid content.Further, a need has arisen for improved methods and systems for theproduction of a protein product (e.g., a high-concentration proteinproduct) in a manner requiring decreased water expenditures.

The present disclosure relates, in some embodiments, to methods andsystems for processing a protein product (e.g., a high-concentrationprotein product) from a microcrop (e.g., aquatic species, Lemna) andcompositions thereof. A method may comprise, for example, blanching aharvested biomass to form a blanched biomass, drying the blanchedbiomass to form a dried biomass, and milling the dried biomass to form ahigh-concentration protein product (e.g., a protein concentrate flour, adry milled protein concentrate).

According to some embodiments, the present disclosure relates to amethod of processing a biomass comprising a microcrop, where the methodmay include: blanching a first portion of the biomass in a blanchingsolution to form a wet protein concentrate; separating the first wetprotein concentrate from a separated solution (e.g., using a screwpress, using a vibratory screen); drying the first wet proteinconcentrate to form at least one of a first protein concentrate flakeand a first protein concentrate granule. A microcrop, in someembodiments, may include at least one of Lemna and Wolffia.

In some embodiments at least one of the first protein concentrate flakeand the first protein concentrate granule may comprise at least 45% DMBprotein, the protein having a Protein Digestibility Corrected Amino AcidScore (PDCAAS) value of at least 0.88. In some embodiments, a PDCAASvalue may be limited by histidine. According to some embodiments, amethod may also include milling at least one of a protein concentrateflake and a protein concentrate granule to form a protein concentrateflour. In some embodiments, a method may include washing a first portionof the biomass with at least one of a first wash solution, a second washsolution, and a third wash solution, where the first wash solution, thesecond wash solution, and the third wash solution may be independentlyselected from a water, a recycled fluid, and an ozonated solution.

In some embodiments, a method may be performed where a blanchingsolution is contacted with a first portion of a biomass at a ratio ofthe blanching solution to a first portion of a biomass of 7:1 (w/w), or6:1 (w/w), or 5:1 (w/w), or (4:1 (w/w). Blanching a first portion of abiomass, in some embodiments, may include combining the first portion ofthe biomass and a blanching solution at a product flow rate ratio of 7:1(w/w) (blanching solution to biomass). According to some embodiments,blanching a biomass may include exposing the biomass to the blanchingsolution for less than 1 min. A method, according to some embodiments,may include exposing a biomass to a blanching solution for about 45 sec.In some embodiments, blanching a biomass may include contacting at leastone surface of the biomass with a blanching solution. According to someembodiments, blanching a first portion of a biomass may compriseexposing the biomass to a blanching solution for less than 2 min wherethe blanching solution may have a temperature between about 75° C. and95° C. A blanching solution, in some embodiments, may include at leastone calcium salt. According to some embodiments, a method may includecooling a wet protein concentrate.

According to some embodiments, a method of processing a biomasscomprising a microcrop may include solvent extracting a wet proteinconcentrate. In some embodiments, a wet protein concentrate may beseparated from a separated solution using a vibratory screen (e.g.,before solvent extraction).

A method of processing a biomass comprising a microcrop may includerecycling a separated solution by performing at least one of: dilutingthe separated solution, filtering the separated solution, and monitoringthe separated solution. In some embodiments, a method may includeblanching a second portion of a biomass in a blanching solution or arecycled blanching solution to form a second wet protein concentrate;separating the second wet protein concentrate from the separatedsolution; and drying the second wet protein concentrate to form at leastone of a second protein concentrate flake and a second proteinconcentrate granule. In some embodiments, at least one of a secondprotein concentrate flake and a second protein concentrate granule maycomprise at least 45% DMB protein, the protein having a PDCAAS value ofat least 0.88.

The present disclosure further relates, according to some embodiments,to a high-concentration protein product generated by processing abiomass comprising a microcrop (e.g., Lemna, Wolffia) where theprocessing method may include: blanching a first portion of the biomassin a blanching solution to form a wet protein concentrate; separatingthe first wet protein concentrate from a separated solution; and dryingthe first wet protein concentrate to form at least one of a firstprotein concentrate flake and a first protein concentrate granule. Insome embodiments, at least one of the first protein concentrate flakeand the first protein concentrate granule may comprise at least 45% DMBprotein, the protein having a PDCAAS value of at least 0.88. Accordingto some embodiments, a PDCAAS value may be limited by histidine. In someembodiments, at least one of a protein concentrate flake and a proteinconcentrate granule may be milled to form a protein concentrate flour.

In some embodiments, at least one of a protein concentrate flake and/ora protein concentrate granule may have at least one of the followingcharacteristics: a PDCAAS of at least 0.92, a digestibility of at least90%, an ash content of less than 10% DMB, a dietary fiber content of atleast 30%, an oxalic acid content of less than 1% DMB, a polyphenolcontent of less of less than 3.2 mg/100 g, a fat content of less than7%, a water-binding capacity of at least 7 ml/g, and an oil-bindingcapacity of at least 3 ml/g. In some embodiments, at least one of aprotein concentrate flake and a protein concentrate granule may have anoxalic acid content of less than 0.25% DMB, a polyphenol content of lessof less than 1.75 mg/100 g, or both.

According to some embodiments, a method of processing a biomasscomprising a microcrop may include solvent extracting a wet proteinconcentrate. In some embodiments, a wet protein concentrate may beseparated from a separated solution using a vibratory screen (e.g.,before solvent extraction). A high-concentration protein productproduced by a method including solvent extraction may generate at leastone of a protein concentrate flake and a protein concentrate granulehaving at least one of the following characteristics: a protein contentof at least 50%, a PDCAAS of at least 0.92, a reduced chlorophyllconcentration, a digestibility of at least 90%, an ash content of lessthan 10% DMB, a dietary fiber content of at least 30%, an oxalic acidcontent of less than 1% DMB, a polyphenol content of less of less than3.2 mg/100 g, a fat content of less than 5%, a water-binding capacity ofat least 7 ml/g, and an oil-binding capacity of at least 3 ml/g. In someembodiments, at least one of the protein concentrate flake and a proteinconcentrate granule generated by a method including solvent extractionmay have an oxalic acid content of less than 0.25% DMB, a polyphenolcontent of less of less than 1.75 mg/100 g, or both.

Some embodiments of the present disclosure relate to a method ofprocessing a biomass comprising a microcrop where the method includes:blanching the first portion of the biomass in a blanching solution toform a first wet protein concentrate; separating the first wet proteinconcentrate from a separated solution; milling the first wet proteinconcentrate to form a first milled wet protein concentrate; and dryingthe first milled wet protein concentrate to form a first dry milledprotein concentrate. In some embodiments, a first dry milled proteinconcentrate may comprise at least 45% DMB protein, the protein having aPDCAAS value of at least 0.88. According to some embodiments, a PDCAASvalue of a first dry milled protein concentrate may be limited byhistidine.

In some embodiments, a method of generating a first dry milled proteinconcentrate may be performed where a ratio of the blanching solution toa first portion of a biomass is 7:1 (w/w), or 6:1 (w/w), or 5:1 (w/w),or (4:1 (w/w). Blanching a first portion of a biomass, in someembodiments, may include combining the first portion of the biomass anda blanching solution at a product flow rate ratio of 7:1. According tosome embodiments, blanching a biomass may include exposing the biomassto the blanching solution for less than 1 min. A method, according tosome embodiments, may include exposing a biomass to a blanching solutionfor about 45 sec. In some embodiments, blanching a biomass may includecontacting at least one surface of the biomass with a blanchingsolution. According to some embodiments, blanching a first portion of abiomass may comprise exposing the biomass to a blanching solution forless than 2 min where the blanching solution may have a temperaturebetween about 75° C. and 95° C. A blanching solution, in someembodiments, may include at least one calcium salt.

According to some embodiments, a method of processing a biomass togenerate a first dry milled protein concentrate may include solventextracting a wet protein concentrate. In some embodiments, a wet proteinconcentrate may be separated from a separated solution using a vibratoryscreen (e.g., before solvent extraction).

A method of processing a biomass comprising a microcrop to generate afirst dry milled protein concentrate may include recycling a separatedsolution by performing at least one of: diluting the separated solution,filtering the separated solution, and monitoring the separated solution.In some embodiments, a method may include blanching a second portion ofthe biomass in a blanching solution or a recycled blanching solution toform a second wet protein concentrate; separating the second wet proteinconcentrate from the separated solution; milling a second portion of thewet protein concentrate to form a second milled wet protein concentrate;and drying the second milled wet protein concentrate to form a seconddry milled protein concentrate. In some embodiments, a second dry milledprotein concentrate may comprise at least 45% DMB protein, the proteinhaving a PDCAAS value of at least 0.88.

Further, the present disclosure relates, in some embodiments, to aprotein composition comprising at least one high-concentration proteinproduct extracted from a microcrop (e.g., Lemna, Wolffia) and at leastone medium, where the at least one high-concentration protein productincludes at least one of a protein concentrate flake, a proteinconcentrate granule, a protein concentrate flour, or a dry milledprotein concentrate, and comprises at least 45% DMB protein, the proteinhaving a Protein Digestibility Corrected Amino Acid Score (PDCAAS) valueof at least 0.88. According to some embodiments, a PDCAAS value may belimited by histidine. A protein composition may be selected from ashake, a smoothie, a nutrition bar, and an animal feed product, in someembodiments.

According to some embodiments, at least one of a protein concentrateflake, a protein concentrate granule, a protein concentrate flour, or adry milled protein concentrate of a protein composition may have atleast one of: a protein content of at least 50%, a PDCAAS of at least0.92, a reduced chlorophyll concentration, a digestibility of at least90%, an ash content of less than 10% DMB, a dietary fiber content of atleast 30%, an oxalic acid content of less than 1% DMB, a polyphenolcontent of less of less than 3.2 mg/100 g, a fat content of less than5%, a water-binding capacity of at least 7 ml/g, and an oil-bindingcapacity of at least 3 ml/g. In some embodiments, at least one of aprotein concentrate flake, a protein concentrate granule, a proteinconcentrate flour, or a dry milled protein concentrate of a proteincomposition may further comprise an oxalic acid content of less than0.25% DMB, a polyphenol content of less of less than 1.75 mg/100 g, orboth.

In some embodiments, a protein composition may include at least oneadditive. An additive may be selected from a sweetener, a hydrocolloidalstabilizer, a flavor, a nutritional component, or any combinationthereof, according to some embodiments.

BRIEF DESCRIPTION OF THE DRAWINGS

The file of this patent contains at least one drawing executed in color.Copies of this patent with color drawing(s) will be provided by thePatent and Trademark Office upon request and payment of the necessaryfee.

Some embodiments of the disclosure may be understood by referring, inpart, to the present disclosure and the accompanying drawings, wherein:

FIG. 1A is a flow diagram illustrating a process for cultivating,harvesting, and processing a microcrop for the production ofhigh-concentration protein product according to a specific exampleembodiment of the disclosure;

FIG. 1B is a flow diagram illustrating a process for cultivating,harvesting, and processing a microcrop for the production ofhigh-concentration protein product according to a specific exampleembodiment of the disclosure;

FIG. 1C is a flow diagram illustrating a process for cultivating,harvesting, and processing a microcrop for the production ofhigh-concentration protein product according to a specific exampleembodiment of the disclosure;

FIG. 1D is a flow diagram illustrating a process for cultivating,harvesting, and processing a microcrop for the production ofhigh-concentration protein product according to a specific exampleembodiment of the disclosure;

FIG. 2A is a flow diagram illustrating a system for cultivating,harvesting, and processing a microcrop for the production ofhigh-concentration protein product according to a specific exampleembodiment of the disclosure;

FIG. 2B is a flow diagram illustrating a system for cultivating,harvesting, and processing a microcrop for the production ofhigh-concentration protein product according to a specific exampleembodiment of the disclosure;

FIG. 2C is a flow diagram illustrating a system for cultivating,harvesting, and processing a microcrop for the production ofhigh-concentration protein product according to a specific exampleembodiment of the disclosure; and

FIG. 2D is a flow diagram illustrating a system for cultivating,harvesting, and processing a microcrop for the production ofhigh-concentration protein product according to a specific exampleembodiment of the disclosure.

DETAILED DESCRIPTION

The present disclosure relates, in some embodiments, to a method ofprocessing a biomass comprising a microcrop, the method may include: (a)optionally washing a first portion of the biomass with at least one of afirst wash solution, a second wash solution, and a third wash solution,(b) blanching the first portion of the biomass in a blanching solutionto form a wet protein concentrate, wherein the blanching solutionoptionally comprises at least one calcium salt; (c) optionally coolingthe wet protein concentrate; (d) optionally filtering a blanchingsolution to form a filtered blanching solution and a blanching waste;(e) if (d) is included, optionally recycling at least one of thefiltered blanching solution and the blanching waste; (f) optionallyextracting the wet protein concentrate with a solvent solution; (g) if(f) is included, optionally recovering a solvent and a byproduct fromthe solvent solution, wherein the byproduct comprises at least one of achlorophyll byproduct and a fat byproduct; (h) optionally milling afirst portion of the wet protein concentrate to form a milled wetprotein concentrate; (i) if (h) is included, drying the milled wetprotein concentrate to form a dry milled protein concentrate; (j) dryinga second portion of the wet protein concentrate to form a proteinconcentrate flake; and/or (k) milling the protein concentrate flake toform a protein concentrate flour. According to some embodiments, atleast one of the protein concentrate flour and the dry milled proteinconcentrate may comprise: (i) at least 40% protein dry mass basis (DMB),(ii) at least 5% DMB of at least one of an apiogalacturonan and/or anoligogalacturonide, and/or (iii) optionally an oxalic acid content of≤0.05% DMB. In some embodiments, at least one of the protein concentrateflour and the dry milled protein concentrate may comprise: (i) at least60% DMB protein, (ii) at least 5% DMB of at least one of anapiogalacturonan and/or an oligogalacturonide, and/or (iii) optionallyan oxalic acid content of ≤0.05%. According to some embodiments, atleast one of a protein concentrate flour and a dry milled proteinconcentrate may have reduced chlorophyll (e.g., decolored). In someembodiments, a microcrop may comprise Lemna.

Further, the present disclosure relates to a system of processing abiomass comprising a microcrop to generate a high-protein concentrate,the system, in some embodiments, may comprise: (a) optionally a washingunit configured to wash a first portion of the biomass with at least oneof a first wash solution, a second wash solution, and a third washsolution, (b) a blanching unit configured to blanch the first portion ofthe biomass in a blanching solution to form a wet protein concentrate;(c) a first separation unit configured to separate the blanchingsolution from the wet protein concentrate; (d) optionally a cooling unitconfigured to cool the wet protein concentrate; (e) a second separationunit configured to separate the cooling liquid from the wet proteinconcentrate; (f) optionally a filtering unit configured to separate theblanching solution to form a filtered blanching solution and a blanchingwaste; (g) optionally a solvent extraction unit configured to extractthe wet protein concentrate with a solvent solution; (h) optionally amilling unit configured to mill at least a portion of the wet proteinconcentrate to form a milled wet protein concentrate; (i) a drying unitconfigured to dry at least a portion of the wet protein concentrateand/or the milled wet protein concentrate (e.g., to produce a proteinconcentrate flake), and/or (j) if (h) is excluded, a milling unitconfigured to mill at least a portion of the dried protein concentrateto form a protein concentrate flour.

Additionally, some embodiments of the present disclosure relate to acomposition comprising at least 40% protein, at least 5% DMB of at leastone of an apiogalacturonan and/or an oligogalacturonide, and/oroptionally an oxalic acid content of ≤0.05%. In some embodiments, acomposition may comprise: at least 60% protein, at least 5% DMB of atleast one of an apiogalacturonan and/or an oligogalacturonide, and anoxalic acid content of ≤0.05%.

The present disclosure relates, in some embodiments, to methods andsystems for processing a high-concentration protein product (e.g., ≥45%DMB,) from a microcrop (e.g., aquatic species, Lemna, Wolffia) andcompositions thereof. More specifically, the present disclosure relates,in some embodiments, to methods and systems for processing ahigh-concentration protein product from Lemna and/or Wolffia. In someembodiments, the present disclosure relates to compositions of ahigh-concentration microcrop protein product processed from an aquaticspecies.

The present disclosure relates to compositions, systems, and methods forproducing a high-concentration (e.g., ≥45% DMB) protein concentrate(e.g., wet, flakes, granules, flour) from a microcrop (e.g., aquaticplant species, Lemna, Wolffia, algal species). For example, a method maycomprise cultivating, harvesting, washing, blanching, dewatering,separating, drying, and/or milling a microcrop (e.g., aquatic plantspecies, Lemna, algal species) for the production of ahigh-concentration (e.g., ≥60% DMB, ≥45% DMB) protein concentrate (e.g.,wet, flakes, granules, flour) according to specific example embodimentsof the disclosure. A method may be performed, in some embodiments, in aseries of steps, one or more of which may be repeated. For example, amethod may comprise a single cycle (e.g., no step is repeated) resultingin the production of high-concentration (e.g., ≥45% DMB) proteinconcentrate (e.g., wet, flakes, granules, flour). In some embodiments, amethod may comprise multiple cycles (e.g., first portion, secondportion) or a continuous process for the production ofhigh-concentration (e.g., ≥45% DMB) protein concentrate (e.g., wet,flakes, granules, flour) such that products, intermediates and/orbyproducts of an earlier cycle of the process may be recycled into oneor more subsequent cycles of the process.

Microcrop

In some embodiments, a microcrop may comprise a single aquatic species(e.g., Lemna species, Salvinia species). A microcrop may include speciesof Lemna (e.g., duckweed), Spirodela, Landoltia, Wolfiella, Salvinia(e.g., floating fern), Wolffia (e.g., watermeal), Azolla (e.g., mosquitofern), Pistia (e.g., water lettuce), or any combination thereof.According to some embodiments, a microcrop may be a species of Lemna,for example, Lemna minor, Lemna obscura, Lemna minuta, Lemna gibba,Lemna valdiviana, or Lemna aequinoctialis. A microcrop may comprise,according to some embodiments, a combination of two or more aquaticspecies. In some embodiments, a microcrop may be selected from a localaquatic species based on identified compositional and growthcharacteristics that have developed within the local environmentalconditions. Local species may out-compete other species in open ponds orbioreactors based on their adaptation to the local environmentalconditions. A microcrop, in some embodiments, may be adjusted inresponse to seasonal variations in temperature and light availability.

A microcrop may have characteristics that are advantageous in comparisonto other aquatic species (e.g., rapid growth rate; reduced nutritionalrequirements; ease of harvesting and/or processing; enhanced amino acidprofile; enhanced palatability; reduced evapotranspiration rate;increased protein composition).

For example, Lemna is a genus of free-floating aquatic plants from theLemnaceae family (e.g., duckweed) that grow rapidly. Lemna protein hasan essential amino acid profile that more closely resembles animalprotein than most other plant proteins. Table 1 shows a typicalessential amino acid compositional profile of Lemna protein.Additionally, Lemna provides high protein yields, with freshly harvestedLemna containing up to about 43% protein by dry weight. Furthermore,compared with most other plants, Lemna leaves have a low fiber content(e.g., about 5%-about 15% in dry matter) and are highly digestible, evenfor monogastric animals. This contrasts with the compositions of manycrop species (e.g., soy beans, rice, maize) which have fiber contents ofapproximately 50% and low digestibility.

TABLE 1 Essential Amino Acid Profile of Lemna Protein Essential AminoAcid Protein (g/100 g) Lysine 5.9 Leucine 9.7 Isoleucine 5.1 Methionine2.4 Phenylalanine 6.3 Threonine 4.4 Tryptophan 2.0 Valine 6.3 Histidine2.7 Arginine 6.8Cultivation of a Microcrop

In some embodiments a microcrop may be asexually propagated (e.g.,cultivated) by contacting the microcrop with a first medium (e.g., anaqueous nutrient composition, a growth medium) under conditions thatpermit expansion. A microcrop may be cultivated in a bioreactor system,according to some embodiments. A bioreactor system may contain a firstmedium (e.g., a growth medium) comprising water and/or a nutrientcomposition, according to some embodiments. A nutrient composition, insome embodiments, may include at least one of nitrogen, phosphorus,potassium, and calcium. In some embodiments, a first medium may comprisedissolved gaseous oxygen and/or dissolved gaseous carbon dioxide.According to some embodiments, a first medium may be configured to havean increased calcium composition (e.g., an increased calcium growthmedium). For example, an increased calcium first medium may comprise acalcium concentration of ≥about 120 parts per million (ppm), or ≥about115 ppm, or ≥about 110 ppm, or ≥about 105 ppm, or ≥about 100 ppm, or≥about 95 ppm, or ≥about 90 ppm, or ≥about 85 ppm, or ≥about 80 ppm, or≥about 75 ppm, or ≥about 70 ppm, or ≥about 65 ppm, or ≥about 60 ppm, or≥about 55 ppm, or ≥about 50 ppm, or ≥about 45 ppm, or ≥about 40 ppm, or≥about 35 ppm, or ≥about 30 ppm, or ≥about 25 ppm, or ≥about 20 ppm,where “about” may constitute plus or minus 10%. In some embodiments, anincreased calcium first medium may comprise a calcium concentration ofabout 20 ppm to about 120 ppm, about 25 ppm to about 120 ppm, or about30 ppm to about 120 ppm, or about 40 ppm to about 120 ppm, or about 50ppm to about 120 ppm, or about 60 ppm to about 120 ppm, or about 70 ppmto about 120 ppm, or about 80 ppm to about 120 ppm, or about 20 ppm toabout 100 ppm, or about 30 ppm to about 100 ppm, or about 40 ppm toabout 100 ppm, or about 50 ppm to about 100 ppm, or about 60 ppm toabout 100 ppm, or about 70 ppm to about 100 ppm, or about 80 ppm toabout 100 ppm. An increased calcium first medium, according to someembodiments, may comprise a calcium concentration of at least about 20ppm (e.g., ±10%). In some embodiments an increased calcium first mediumcomprises at least 100 ppm calcium. A bioreactor system may beconfigured to insert additional nutrients (e.g., nitrogen, phosphorus,potassium, calcium) or gases (e.g., oxygen; carbon dioxide) into thefirst medium at specified time indicators or in response to sensorreadings. In some embodiments, a calcium may comprise calcium, calciumcarbonate, calcium oxalate, calcium oxide, calcium citrate, calciumcarbide, calcium phosphate, calcium sulfate, calcium chloride, orcombinations thereof.

In some embodiments, a first medium may comprise one or moreanti-photosynthetic dyes that are configured to attenuatephotosynthetically active radiation within the growth medium. The one ormore anti-photosynthetic dyes may be added at a sufficient volume orconcentration to inhibit growth of at least one other aquatic organism(e.g., submerged aquatic species, phytoplankton, phytoalgae, epiphyticalgae), according to some embodiments. An anti-photosynthetic dye mayinclude at least one of(n-ethyl-n-[4-[[4-[ethyl[(3-sulfophenyl)methyl]amino]-phenyl](2-sulfophenyl)-methylene)]2,5-cyclohexadien-1-ylidene]-3-sulfobenzenemethanaminiumhydroxide inner salt, disodium salt, (Colour Index Acid Blue 9 (Ref. No.42090)), trisodium(4E)-5-oxo-1-(4-sulfonatophenyl)-4-[(4-sulfonatophenyl)hydrazono]-3-pyrazolecarboxylate(Colour Index Acid Yellow 23 (Ref. No. 19140)), diazanium;2-[[4-[ethyl-[(3-sulfonatophenyl)methyl]amino]phenyl]-[4-[ethyl-[(3-sulfonatophenyl)methyl] azaniumylidene] cyclohexa-2,5-dien-1-ylidene] methyl]benzenesulfonate (Colour Index Acid Blue 34 (Ref. No. 42645));benzyl-[4-[[4-[benzyl(ethyl)amino]phenyl]-(5-hydroxy-2,4-disulfophenyl)methylidene]cyclohexa-2,5-dien-1-ylidene]-ethylazanium(Colour Index Acid Blue 5 (Ref. No. 42052));disodium-2-(1,3-dioxoinden-2-yl)quinoline-6,8-disulfonate (Colour IndexAcid Yellow 3 (Ref. No. 15985)), and a mixture of(n-ethyl-n-[4-[[4-[ethyl[(3-sulfophenyl)methyl]amino]-phenyl](2-sulfophenyl)-methylene)]2,5-cyclohexadien-1-ylidene]-3-sulfobenzenemethanaminiumhydroxide inner salt, disodium salt and trisodium(4E)-5-oxo-1-(4-sulfonatophenyl)-4-[(4-sulfonatophenyl)hydrazono]-3-pyrazolecarboxylate(Aquashade®). Other suitable anti-photosynthetic dyes may be found inTables I and II of U.S. Pat. No. 4,042,367 to Wilson, which isincorporated herein by reference.

A first medium (e.g., an aqueous nutrient composition) may be providedin and/or added to a bioreactor (e.g., a pond) and may be maintained ata desired set-point level (e.g., specific volume), according to someembodiments. A bioreactor system, in some embodiments, may be configuredto collect rainfall and/or to intake water from a source of ground,surface, or recycled water (e.g., storm water, recycled water) or anyother suitable water source. According to some embodiments, a bioreactorsystem may further comprise an additional storage container (e.g.,container or pond) for excess growth medium.

In some embodiments, one or more smaller bioreactors (e.g., pond) may bedesigned and sized to adequately serve as “feeder” bioreactors to alarger bioreactor. Smaller bioreactors, in some embodiments, may befirst inoculated and grown to high density at which point they mayoptimally seed a larger bioreactor in a manner that supports fastergrowth.

In some embodiments, a bioreactor system may comprise a monitoringsystem. A monitoring system may be configured to display and/or provideone or more user alerts regarding bioreactor condition(s) (e.g.,nutrient concentrations, pH, dissolved oxygen levels, growth mediumlevels, microcrop distribution, flow rate, temperature) and/or adjustoperating conditions (e.g., growth medium flow rate and/or timing and/orquantity of nutrient addition; “feeder” microcrop addition, oxygen orcarbon dioxide addition), in some embodiments. Adjustments may be madecontinuously, semi-continuously, periodically, intermittently, asneeded, at set or variable times, or any other interval. In someembodiments, adjustments may be selected to optimize growth rates and/oryield of the aquatic species. For example, a microcrop species may begrown in large-scale, open bioreactors with monitoring systemsconfigured to adjust the introduction of materials (e.g., fresh orrecycled water, fresh or recycled growth media) based on, for example,exposure to light, which may thereby regulate nutrient consumptionrates.

A bioreactor system may comprise, in some embodiments, a singlecontainer in which the microcrop may be cultivated. In some embodiments,the bioreactor system may comprise multiple cultivation containers thatmay be connected, partially connected, or disconnected. A bioreactor(e.g., a pond), in some embodiments, may be an earthen basin with theembankments made of compacted dirt removed from the interior bottom ofthe bioreactor. According to some embodiments the bioreactor may be anartificial container (e.g., metal, plastic, resin). A bioreactor systemmay comprise an open bioreactor, a closed bioreactor, a semi-openbioreactor, or any combination thereof. In some embodiments, abioreactor system may be configured to divide the container(s) intochannels or cells. A bioreactor system may be configured to permit aflow of growth medium, in some embodiments. A bioreactor system, in someembodiments, may include a propulsion system (e.g., paddle wheels,bubbling, submerged or surface water jets, submerged mixers) and/or arecirculation system. In some embodiments, a bioreactor system may beconfigured to adjust the flow rate of a growth medium (e.g., toredistribute nutrient concentrations or microcrop growth patterns).

In some embodiments a bioreactor system may be open (e.g., in ahorizontal plane relative to the ground) of a bioreactor container(e.g., serpentine raceway) such that a growth medium contained withinthe bioreactor container and/or a microcrop growing on a top surface ofthe growth medium may be exposed to a wind initiating from an exteriorof the bioreactor container. A bioreactor system, according to someembodiments, may be partially open (e.g., in a horizontal plane relativeto the ground) with at least 90% or at least 80%, or at least 70%, or atleast 60%, or at least 50%, or at least 40%, or at least 30%, or atleast 20%, or at least 10% of the top surface of the contained culturemedia being open. A top surface may be open, according to someembodiments, where the surface is substantially free (e.g., free) of anycovering or other barrier, where the surface is directly exposed toambient weather conditions, where there is substantially no membrane,glass, cover or other barrier (whether or not such barrier has pores orapertures) between the surface and the atmosphere, and/or where ambientatmosphere is the only occupant of the space immediately and directlyabove the surface for a distance of at least about 1 meter above thesurface.

A bioreactor system, in some embodiments, may monitor and adjust athickness and distribution of a microcrop mat. For example, when amicrocrop reaches a specified thickness or distribution a bioreactorsystem may initiate harvest procedures. In some embodiments, a minimumthickness of a microcrop mat may be maintained such that a desiredevapotranspiration rate of a growth medium within a bioreactor systemmay be maintained. A minimum thickness of a microcrop may be maintained,in some embodiments, such that less sunlight is capable of penetrating asurface of a growth medium (i.e., reducing a growth potential ofsubmerged aquatic species such as algae).

A microcrop may be cultivated by any suitable method and is not limitedto the method described herein. Various changes may be made in themethod of cultivation of a microcrop without departing from the scope ofthe instant disclosure.

Harvesting of a Microcrop

A microcrop may be harvested in whole or in part at any desired time(s)to form a biomass. For example, a microcrop may be harvested at one ormore specific times, at regular or irregular intervals and/orcontinuously. Selection of harvest time(s) and/or intervals may be basedon environmental conditions (e.g., precipitation, relative humidity,temperature range, average, low or high threshold and/or lightintensity, wavelength range, duration of exposure) and/or the microcropexhibiting one or more desired characteristics (e.g., mat thickness, matdistribution, maturation). Harvesting a microcrop may be manual orautomated. In some embodiments, an automated skimmer system may collecta microcrop from a bioreactor system and transfer a harvested microcrop(e.g., via a pumping system) onto an inclined vibrating screen toseparate a biomass from growth medium and debris. A microcrop, in someembodiments, may be harvested by vacuum skimming the microcrop from thebioreactor system through a stationary or mobile screen filter.According to some embodiments, a biomass slurry, including a harvestedmicrocrop (e.g., Lemna) and a growth medium (e.g., water), may beconveyed to an inclined vibrating screen where a biomass (e.g.,microcrop) may be separated from the growth medium.

During harvesting, a separated growth medium may be recycled back intothe bioreactor system or to an additional storage container (e.g.,container or pond), according to some embodiments. In some embodiments,at least about 40%, or at least about 50%, or at least about 60%, or atleast about 70%, or at least about 80%, or at least about 90%, or atleast about 95% of a growth medium (e.g., water) separated from abiomass may be recycled for further use in cultivating, harvesting,and/or processing a microcrop.

Soaking a Biomass and/or Buffering a pH of a Biomass

After harvesting, a biomass may be soaked and/or buffered. Soakingand/or buffering a harvested biomass may contribute to a reduction in anoxalic acid content of a protein product. In some embodiments, soakingand/or buffering a harvested biomass may contribute to a reduction in anoxalic acid and/or oxalate content of a protein product.

In some embodiments, a harvested biomass may be soaked in a secondmedium. A second medium may comprise water (e.g., ground water, surfacewater, recycled water), distilled water, reverse osmosis or nanofilteredwater, and/or a nutrient composition, according to some embodiments. Insome embodiments, a second medium may comprise any desired portion ofrecycled fluid. For example, a second medium may comprise at least about10% (v/v), at least about 20% (v/v), at least about 30% (v/v), at leastabout 40% (v/v), at least about 50% (v/v), at least about 60% (v/v), atleast about 70% (v/v), at least about 80% (v/v), or at least about 90%(v/v) recycled fluid from another stage of the process.

According to some embodiments, a second medium may be configured to havea low nitrogen composition (e.g., a low nitrogen second medium). Forexample, a low nitrogen second medium may comprise a nitrogenconcentration of <about 20 parts per million (ppm), <about 18 ppm,<about 16 ppm, or <about 14 ppm, or <about 12 ppm, or <about 10 ppm, or<about 9 ppm, or <about 8 ppm, or <about 7 ppm, or <about 6 ppm, or<about 5 ppm, or <about 4 ppm, or <about 3 ppm, or <about 2 ppm, or<about 1 ppm, or <about 0.5 ppm, or about 0 ppm. In some embodiments, alow nitrogen second medium may comprise a nitrogen concentration ofabout 0 ppm to about 20 ppm, or about 0.5 ppm to about 20 ppm, or about0.5 ppm to about 15 ppm, or about 0.5 ppm to about 10 ppm, or about 1ppm to about 9 ppm, or about 1 ppm to about 7 ppm, or about 1 ppm toabout 6 ppm, or about 1 ppm to about 5 ppm, or about 3 ppm to about 6ppm, or about 2 ppm to about 8 ppm. A low nitrogen second medium,according to some embodiments, may comprise a nitrogen concentration ofat most about 10 ppm (e.g., ±1 ppm). In some embodiments, a low nitrogensecond medium may comprise a nitrogen concentration of at most about 5ppm (e.g., ±0.5 ppm). A low nitrogen second medium comprises at leastsome quantity of nitrogen in contrast to, for example, a no nitrogensecond medium having no detectable nitrogen (i.e., N₂). In someembodiments, a second medium may be a no nitrogen second medium.

According to some embodiments, a second medium may be configured to havea low calcium composition (e.g., a low calcium second medium). Forexample, a low calcium second medium may comprise a calciumconcentration of ≤about 20 ppm, ≤about 18 ppm, ≤about 16 ppm, or ≤about14 ppm, or ≤about 12 ppm, or ≤about 10 ppm, or ≤about 9 ppm, or ≤about 8ppm, or ≤about 7 ppm, or ≤about 6 ppm, or ≤about 5 ppm, or ≤about 4 ppm,or ≤about 3 ppm, or ≤about 2 ppm, or ≤about 1 ppm, or ≤about 0.5 ppm, orabout 0 ppm. In some embodiments, a low calcium second medium maycomprise a calcium concentration of about 0 ppm to about 20 ppm, orabout 0.5 ppm to about 20 ppm, or about 0.5 ppm to about 15 ppm, orabout 0.5 ppm to about 10 ppm, or about 1 ppm to about 9 ppm, or about 1ppm to about 7 ppm, or about 1 ppm to about 6 ppm, or about 1 ppm toabout 5 ppm, or about 3 ppm to about 6 ppm, or about 2 ppm to about 8ppm. A low calcium second medium, according to some embodiments, maycomprise a calcium concentration of at most about 10 ppm (e.g., ±1 ppm).In some embodiments, a low calcium second medium may comprise a calciumconcentration of at most about 5 ppm (e.g., ±0.5 ppm). In someembodiments, soaking a biomass in a low calcium second medium may effectthe equilibrium between an oxalic acid concentration and an oxalateconcentration (e.g., calcium oxalate).

In some embodiments, a second medium may be configured to have a highcalcium composition (e.g., a high calcium second medium). For example, ahigh calcium second medium may comprise a calcium concentration of≤about 800 ppm, or ≤about 750 ppm, or ≤about 700 ppm, or ≤about 650 ppm,or ≤about 600 ppm, or ≤about 550 ppm, or ≤about 500 ppm, or ≤about 450ppm, or ≤about 400 ppm, or ≤about 350 ppm, or ≤about 300 ppm, or ≤about250 ppm, or ≤about 200 ppm, or ≤about 150 ppm, or ≤about 100 ppm, or≤about 50 ppm. In some embodiments, a high calcium second medium maycomprise a calcium concentration of about 50 ppm to about 200 ppm, orabout 50 ppm to about 400 ppm, or about 50 ppm to about 600 ppm, orabout 100 ppm to about 800 ppm, or about 100 ppm to about 700 ppm, orabout 100 ppm to about 600 ppm, or about 100 ppm to about 500 ppm, orabout 300 ppm to about 600 ppm, or about 200 ppm to about 800 ppm. Ahigh calcium second medium, according to some embodiments, may comprisea calcium concentration of at most about 800 ppm (e.g., ±50 ppm). Insome embodiments, a high calcium second medium may comprise a calciumconcentration of at most about 600 ppm (e.g., ±50 ppm). In someembodiments, soaking a biomass in a high calcium second medium mayeffect the equilibrium between an oxalic acid concentration and anoxalate concentration (e.g., calcium oxalate). For example, soaking abiomass in a high calcium second medium may convert oxalic acid intooxalate.

In some embodiments, a second medium may be configured to have a lowcalcium composition and a low nitrogen composition (e.g., a low nitrogenand calcium growth medium). For example, a low nitrogen and calciumgrowth medium may comprise a calcium concentration of ≤about 20 ppm, or≤about 18 ppm, or ≤about 16 ppm, or ≤about 14 ppm, or ≤about 12 ppm, or≤about 10 ppm, or ≤about 9 ppm, or ≤about 8 ppm, or ≤about 7 ppm, or≤about 6 ppm, or ≤about 5 ppm, or ≤about 4 ppm, or ≤about 3 ppm, or≤about 2 ppm, or ≤about 1 ppm, or ≤about 0.5 ppm, or about 0 ppm. A lownitrogen and calcium growth medium may comprise a nitrogen concentrationof ≤about 20 ppm, or ≤about 18 ppm, or ≤about 16 ppm, or ≤about 14 ppm,or ≤about 12 ppm, or ≤about 10 ppm, or ≤about 9 ppm, or ≤about 8 ppm, or≤about 7 ppm, or ≤about 6 ppm, or ≤about 5 ppm, or ≤about 4 ppm, or≤about 3 ppm, or ≤about 2 ppm, or ≤about 1 ppm, or ≤about 0.5 ppm, orabout 0 ppm. In some embodiments, a low nitrogen and calcium secondmedium may comprise a calcium concentration of about 0 ppm to about 20ppm, or about 0.5 ppm to about 20 ppm, or 0.5 ppm to about 15 ppm, or0.5 ppm to about 10 ppm, or about 1 ppm to about 9 ppm, or about 1 ppmto about 7 ppm, or about 1 ppm to about 6 ppm, or about 1 ppm to about 5ppm, or about 3 ppm to about 6 ppm, or about 2 ppm to about 8 ppm. Insome embodiments, a low nitrogen and calcium second medium may comprisea nitrogen concentration of about 0 ppm to about 20 ppm, or about 0.5ppm to about 20 ppm, or 0.5 ppm to about 15 ppm, or 0.5 ppm to about 10ppm, or about 1 ppm to about 9 ppm, or about 1 ppm to about 7 ppm, orabout 1 ppm to about 6 ppm, or about 1 ppm to about 5 ppm, or about 3ppm to about 6 ppm, or about 2 ppm to about 8 ppm. A low nitrogen andcalcium second medium, according to some embodiments, may comprise acalcium concentration of at most about 10 ppm (e.g., ±1 ppm). In someembodiments, a low nitrogen and calcium second medium may comprise acalcium concentration of at most about 5 ppm (e.g., ±0.5 ppm). A lownitrogen and calcium second medium, according to some embodiments, maycomprise a nitrogen concentration of at most about 10 ppm (e.g., ±1ppm). In some embodiments, a low nitrogen and calcium second medium maycomprise a nitrogen concentration of at most about 5 ppm (e.g., ±0.5ppm). In some embodiments, soaking a biomass in a low nitrogen and lowcalcium second medium may effect the equilibrium between an oxalic acidconcentration and an oxalate concentration (e.g., calcium oxalate).

Soaking a biomass may comprise submerging a biomass in a second mediumto form a biomass slurry, according to some embodiments. In someembodiments, a biomass may be soaked for about 1 hour, or about 2 hours,or about 4 hours, or about 6 hours, or about 8 hours, or about 10 hours,or about 12 hours, or about 16 hours, or about 20 hours, or about 24hours, or about 36 hours, or about 48 hours, or about 60 hours, or about72 hours, or about 84 hours, or about 96 hours, or about 108 hours, orabout 120 hours, or about 132 hours, or about 144 hours. Soaking abiomass may include agitation, flow, movement, spraying, or stirring ofa second medium. According to some embodiments, a biomass slurry,including a soaked microcrop (e.g., Lemna) and a second medium (e.g., alow nitrogen second medium), may be conveyed to an inclined vibratingscreen where a biomass (e.g., microcrop) may be separated from thesecond medium.

According to some embodiments a biomass may be buffered in a thirdmedium, according to some embodiments. A third medium may comprise water(e.g., ground water, surface water, recycled water), distilled water,reverse osmosis water and/or nanofiltered water, according to someembodiments. In some embodiments, a third medium may comprise anydesired portion of recycled fluid. For example, a third medium maycomprise at least about 10% (v/v), at least about 20% (v/v), at leastabout 30% (v/v), at least about 40% (v/v), at least about 50% (v/v), atleast about 60% (v/v), at least about 70% (v/v), at least about 80%(v/v), or at least about 90% (v/v) recycled fluid from another stage ofthe process.

Buffering a pH of a biomass may comprise submerging a biomass in a thirdmedium to form a biomass slurry, according to some embodiments. In someembodiments, a biomass may be buffered for about 1 hour, or about 2hours, or about 4 hours, or about 6 hours, or about 8 hours, or about 10hours, or about 12 hours, or about 16 hours, or about 20 hours, or about24 hours, or about 36 hours, or about 48 hours. According to someembodiments, a biomass slurry, including a buffered microcrop (e.g.,Lemna) and a third medium (e.g., distilled water, ground water, surfacewater, rain water), may be conveyed to an inclined vibrating screenwhere a biomass (e.g., microcrop) may be separated from the thirdmedium. In other embodiments, a biomass (e.g., microcrop) may beseparated from the third medium by draining.

According to some embodiments, buffering a pH of a biomass may includechanging (e.g., raise, lower) or maintaining a pH value of the biomass.In some embodiments, buffering a biomass may comprise changing (e.g.,raising, lowering) or maintaining a pH value of a biomass to below about8.0, or below about 7.5, or below about 7.0, or below about 6.5, orbelow about 6.0, or below about 5.5, or below about 5.0, or below about4.5, or below about 4.0, or below about 3.5, or below about 3.0.According to some embodiments, buffering a biomass may comprise changing(e.g., raising, lowering) or maintaining a pH value of a biomass to arange of: from about 3.0 to about 7.5, or from about 3.5 to about 7.5,or from about 4.0 to about 7.5, or from about 4.5 to about 7.5, or fromabout 5.0 to about 7.5, or from about 5.5 to about 7.5, or from about6.0 to about 7.5, or from about 6.5 to about 7.5. As would beappreciated by someone having ordinary skill in the art, buffering abiomass by adjusting a pH value of a biomass may promote proteinstability which may, in some embodiments, promote greater protein yieldsin comparison to a non-buffered biomass.

One or more of a soaked biomass and a buffered biomass generated in oneprocedure may be stored in their respective container (e.g., soakingcontainer, buffering container) before being fed to one or moredownstream procedures or apparatuses. This may accommodate differentoperation schedules or modes including, for example, continuous mode,batch mode, or multiple feeding streams to one or more downstreamprocedure(s) and/or apparatus(es). For example, in some embodiments, abiomass may be harvested during daylight hours and processed (e.g.,soaking and/or buffering), subsequently the processed biomass may befurther processed (e.g., lysing, separating) in smaller batches (e.g., afirst portion, a second portion) to accommodate the capacity limitationsof the downstream processing machinery.

Washing a Biomass

In some embodiments, processing a microcrop or biomass (e.g., firstportion, second portion) may include a wash procedure (e.g., FIG. 1B106, FIG. 2B 206) to remove excess growth medium, a solvent solution,debris, contaminants, microorganisms, and/or toxins. Washing a biomassmay increase a purity and/or yield of a protein product. A washprocedure may disinfect and/or disinfest a biomass, reducing or removingbacteria, fungi, viruses, insects, and any combination thereof which areon or around the surfaces of the biomass. In some embodiments a washprocedure may be performed by exposing (e.g., submerging, spraying) atleast one surface of a biomass to a wash solution (e.g., water, growthmedium, antimicrobial solution). A wash solution, in some embodiments,may be combined with a biomass (e.g., first portion, second portion) toform a slurry.

In some embodiments, a wash solution may comprise any desired portion ofrecycled fluid. For example, a wash solution may comprise at least about10% (v/v), at least about 20% (v/v), at least about 30% (v/v), at leastabout 40% (v/v), at least about 50% (v/v), at least about 60% (v/v), atleast about 70% (v/v), at least about 80% (v/v), or at least about 90%(v/v) recycled from another stage of the process (e.g., recycled washsolution FIG. 1D 108, filtered blanching solution FIG. 1B 130, FIG. 2B230). In some embodiments a wash solution may be an aqueous solution orsolvent. A wash solution may contain one or more antimicrobials,de-infestation compounds, fatty acids, alcohols, chlorine, oxidizingcompounds, and any combination thereof (e.g., ozonated water).

According to some embodiments a wash solution may be applied at a highpressure. A wash solution may remain in contact with a biomass for atleast about 1 second, or for at least about 5 seconds, or for at leastabout 10 seconds, or for at least about 20 seconds, or for at leastabout 30 seconds, or for at least about 1 minute, or for at least about5 minutes. In some embodiments, a second wash solution (e.g., water,ozonated water, a recycled wash solution (FIG. 1B 108, FIG. 2B 208), afiltered blanching solution (FIG. 1B 130, FIG. 2B 230) may be applied toa biomass. A third wash solution (e.g., water, ozonated water, arecycled wash solution (FIG. 1B 108, FIG. 2B 208), a filtered blanchingsolution (FIG. 1B 130, FIG. 2B 230) may be applied to a biomass, in someembodiments. A composition of a first wash solution, a second washsolution, and a third wash solution may be the same or different fromone another. In some embodiments a first wash solution may be or maycomprise a filtered blanching solution (FIG. 1B 130, FIG. 2B 230), asecond wash solution may be water, and a third wash solution may beozonated water. Some or all of a wash solution (e.g., a first, second,and/or third wash solution), in some embodiments, may be separated froma biomass (e.g., using an inclined screen or vibratory screen).

In some embodiments, some or all of a wash solution, second washsolution, and/or third wash solution may be collected andreused/recycled (e.g., a recycled wash solution (FIG. 1B 108, FIG. 2B208). At least about 40%, or at least about 50%, or at least about 60%,or at least about 70%, or at least about 80%, or at least about 90%, orat least about 95% of a wash solution, second wash solution, and/orthird wash solution (e.g., water) separated from the biomass may berecycled for future use as a recycled wash solution and/or as growthmedium in the bioreactor system (FIG. 1B 108, FIG. 2B 208), according tosome embodiments.

A wash solution, second wash solution, and/or third wash solution, insome embodiments, may have or may be adjusted to have any desired pH.For example, the pH of a wash solution, second wash solution, and/orthird wash solution may be neutral or basic (e.g., about 7.0, or about7.5, or about 8.0, or about 8.5, or about 9.0, or about 9.5, or about10.0). According to some embodiments, the pH of a wash solution, secondwash solution, and/or third wash solution may be from about 7.0 to about7.5, or from about 7.5 to about 8.0, or from about 8.0 to about 8.5, orfrom about 8.5 to about 9.0, or from about 9.0 to about 9.5, or fromabout 9.5 to about 10.0. The pH of a wash solution, second washsolution, and/or third wash solution may be from about 7.0 to about10.0, or from about 7.0 to about 9.5, or from about 7.0 to about 9.0, orfrom about 7.0 to about 8.5, or from about 7.0 to about 8.0, or fromabout 7.0 to about 7.5, in some embodiments.

A wash solution (e.g., a first, second, and/or third wash solution) mayhave a temperature below room temperature (e.g., about 12° C.) at thetime of use. Cooling a wash solution, and thereby the microcrop, mayimprove protein recovery efficiency and/or decrease proteolyticactivity. In some embodiments, a wash solution (e.g., a first, second,and/or third wash solution) may have a temperature below about 30° C.,or below about 20° C., or below about 15° C., or below about 10° C., orbelow about 5° C., or below about 2° C., or below about 1° C., or belowabout 0° C. at the time of use. A wash solution (e.g., a first, second,and/or third wash solution) may have a temperature between about 0° C.and about 10° C., or between about 5° C. and about 15° C., or betweenabout 10° C. and about 20° C., or 15° C. and about 25° C., or betweenabout 20° C. and about 30° C. at the time of use, in some embodiments.

Blanching a Biomass

In some embodiments, processing a microcrop or biomass (e.g., firstportion, second portion) may include blanching a microcrop material(e.g., FIG. 1A 110, FIG. 2A 210) to form a wet protein concentrate(e.g., FIG. 1A 111, FIG. 2A 211). Blanching may be performed, forexample, on a biomass: (1) after harvesting (e.g., FIG. 1A 104, FIG. 2A204); or (2) after harvesting and washing (e.g., FIG. 1C 104/106, FIG.2C 204/206), in some embodiments. According to some embodiments, ablanching procedure may be used either instead of or in addition to awash procedure. Blanching, according to some embodiments, may decreasean ash content, an oxalic acid content, and/or a phenol (e.g., tannin)content of a high-concentration protein product (e.g., wet,flake/granule, flour, a dry milled protein concentrate).

According to some embodiments, blanching may include contacting (e.g.,immersing, submerging) a biomass with a blanching solution. Contacting abiomass, in some embodiments, may include applying (e.g., showering) ablanching solution to at least one surface of the biomass, submergingthe (e.g., completely, partially) biomass, subjecting at least onesurface of the biomass to a wave of the blanching solution. Applying abiomass may include cascading, showering, spraying, misting, fogging,pouring, or dripping the blanching solution, or any combination thereof,in some embodiments. According to some embodiments, a wave of blanchingsolution may include any disturbance on a top surface of a volume ofblanching solution, such as a wave action, a ridge, a swell, or a ripplethat may be capable of depositing any quantity of blanching solutiononto a top surface (i.e., a surface facing away from a bottom surface ofa container holding the blanching solution) of a biomass. In someembodiments, a ratio of a blanching solution to a biomass (w/w) may be10:1, or 9:1, or 8:1, or 7:1, or 6:1, or 5.5:1, or 5:1, or 4.5:1, or4:1, or 3.5:1, or 3:1, or 2.5:1, or 2:1, or 1.5:1, or 1:1.

According to some embodiments, blanching a biomass 110 may be performedat a product flow rate ratio calculated by dividing a pump rate by afeed rate. For example, blanching a biomass may have a product flow rateratio of 7:1 where a blanching solution is transported at a pump rate of28 liters per min (L/min) and a biomass is transported at a feed rate of4 kg per min (kg/min). According to some embodiments, a blanching abiomass may have a product flow rate ratio of about 10:1, or about 9:1,or about 8:1, or about 7.5:1, or about 7:1, or about 6.5:1, or about6:1, or about 5.5:1, or about 5:1, or about 4.5:1, or about 4:1, orabout 3.5:1, or about 3:1, or about 2.5:1, or about 2:1, or about 1.5:1,or about 1:1, according to some embodiments.

A blanching solution may comprise water, surface water, well water,distilled water, reverse osmosis water, and/or nanofiltered water,according to some embodiments. In some embodiments, a blanching solutionmay comprise any desired portion of recycled fluid. For example, ablanching solution may comprise at least about 10% (v/v), at least about20% (v/v), at least about 30% (v/v), at least about 40% (v/v), at leastabout 50% (v/v), at least about 60% (v/v), at least about 70% (v/v), atleast about 80% (v/v), or at least about 90% (v/v) recycled from anotherstage of the process (e.g., recycled blanching solution FIG. 1A 122,FIG. 2A 222). In some embodiments, a blanching solution may furthercomprise at least one calcium salt (e.g., calcium chloride, calciumacetate). Blanching a biomass with a blanching solution comprising atleast one calcium salt (e.g., calcium chloride, calcium acetate) mayremove at least some soluble oxalic acid from a biomass by conversion toinsoluble calcium oxalate. In some embodiments, a calcium salt may beselected from calcium chloride, calcium acetate, calcium carbonate,calcium hydroxide, or a combination thereof.

A blanching solution, in some embodiments, may have a temperature at thetime it contacts a biomass of more than about 60° C., or more than about65° C., or more than about 70° C., or more than about 75° C., or morethan about 80° C., or more than about 85° C., or more than about 90° C.,or more than about 95° C., or more than about 100° C. According to someembodiments, a blanching solution may be in liquid form, gaseous form(e.g., steam) or combinations thereof.

A biomass may be blanched (e.g., contacted with, immersed in, orsubmerged in a blanching solution, steam exposure) for up to about 20sec, or up to about 30 seconds (sec), or up to about 40 sec, or up toabout 50 sec, or up to about 1 min, or up to about 1 min 15 sec, or upto about 1 min 30 sec, or up to about 1 min 45 sec, or up to about 2min, or up to about 2 min 30 sec or up to about 3 min, or up to about 4min, or up to about 5 min, or up to about 6 min, or up to about 7 min,or up to about 8 min, or up to about 9 min, or up to about 10 min,according to some embodiments. In some embodiments, a biomass may beblanched for about 20 sec to about 40 sec, or about 30 sec to about 45sec, or about 30 sec to about 1 min, or about 30 sec to about 1 min 30sec, or about 30 sec to about 2 min, or about 30 sec to about 5 min, orabout 1 min to about 5 min, or about 1 min to about 5 min, or about 1min to about 10 min, or about 30 sec to about 10 min, where “about” mayrepresent plus or minus 10%. According to some embodiments, a biomassmay be blanched at about 85° C. for about 45 sec.

A blanching solution, in some embodiments, may change temperature whilecontacting a biomass. For example, according to some embodiments, abiomass may be contacted by a blanching solution having an initialtemperature of between about 92° C. and about 94° C. where the contactcontinues for a period of about 40 sec at which point the blanchingsolution may have a final contact temperature of between about 75° C.and about 77° C. In some embodiments, a blanching solution, in someembodiments, may have an initial temperature (e.g., a temperature at atime where the blanching solution first contacts a biomass) of more thanabout 60° C., or more than about 65° C., or more than about 70° C., ormore than about 75° C., or more than about 80° C., or more than about85° C., or more than about 90° C., or more than about 95° C., or morethan about 100° C. A blanching solution, in some embodiments, may have afinal contact temperature (e.g., a temperature at a time where thebiomass exits the blanching tray) of less than about 60° C., or lessthan about 65° C., or less than about 70° C., or less than about 75° C.,or less than about 80° C., or less than about 85° C., or less than about90° C., or less than about 95° C., or less than about 100° C.

In some embodiments, some or all of a blanching solution may beseparated from a wet protein concentrate (e.g., FIG. 1A 111). Ablanching solution may be separated from a wet protein concentrate, insome embodiments, using gravity separation, draining, an inclinedscreen, a vibratory screen, filtration, a decanter centrifuge, a beltpress, a fan press, a rotary press, a screw press, a filter press, afinisher press, or any combination thereof, according to someembodiments.

In some embodiment, a separated blanching solution may be collected andreused/recycled (e.g., recycled blanching solution FIG. 1A 122, FIG. 2A222). According to some embodiments, recycling a separated solution mayinclude monitoring a separated solution. According to some embodiments,monitoring a separated solution may include monitoring a composition(e.g., total dissolved solids) and/or temperature of a separatedsolution. Monitoring a composition of a separated solution may includemonitoring one or more of the following: total dissolved solids, totalsolids, turbidity, electrical conductivity, nutrient (e.g., nitrogen)composition, salinity, pH, in some embodiments.

In some embodiments, recycling a separated solution may includemaintaining or adjusting a composition (e.g., total solids, turbidity)of a separated solution. Maintaining or adjusting a composition of aseparated solution, in some embodiments, may include maintaining oradjusting a total solids content of a volume of separated solution at/toa value of less than 0.5% w/w), or less than 1% (w/w) or less than 2%(w/w), or less than 4% (w/w), or less than 6% (w/w) or less than 8%(w/w), or less than 10% (w/w). According to some embodiments,maintaining or adjusting a composition of a separated solution mayinclude maintaining or adjusting a turbidity value (e.g., relative toabsorbance of a 500 nm light source where 1.0 is equivalent to 10%absorbance and 10.0 is equivalent to 100% absorbance) of a volume ofseparated solution at a value of less than about 0.5, or less than about0.75, or less than about 1.0, or less than about 1.25, or less thanabout 1.5, where about may represent plus or minus 5%. In someembodiments, maintaining or adjusting a composition of a separatedsolution may include maintaining or adjusting an electrical conductivityvalue of the separated solution at/to a value of less than about 2000μS/cm, or less than about 2500 μS/cm, or less than about 3000 μS/cm, orless than about 3500 μS/cm, or less than about 4000 μS/cm, or less thanabout 4500 μS/cm, or less than about 5000 μS/cm, or less than about 5500μS/cm, or less than about 6000 μS/cm, where “about” may represent plusor minus 250 μS/cm.

In some embodiments, maintaining or adjusting a composition of aseparated solution may include diluting a separated solution. Dilutionof a separated solution may be desirable to adjust a composition of theseparated solution (e.g., dissolved solids content, turbidity). Adiluted separated solution may be recycled as a blanching solution, as awash solution, as a settling solution, as a cooling solution, or anycombination thereof, in some embodiments.

In some embodiments, diluting a separated solution may involvediscarding a volume of discard solution and adding a volume (e.g., anequal volume) of a dilution solution. A discard solution may have avolume equal to a volume of dilution solution necessary to achieve adesired composition of dissolved solids (e.g., ash), according to someembodiments. In some embodiments, a discard solution may have a volumehigher than a volume of dilution solution necessary to achieve a desiredcomposition of dissolved solids (e.g., ash).

In some embodiments, a discard solution may be recycled as a growthmedium in the cultivation of a microcrop. A dilution solution, accordingto some embodiments, may include water, ground water, well water,distilled water, deionized water, reverse osmosis water, nanofilteredwater, ultra-filtered water, or any combination thereof.

According to some embodiments, a separated solution may be diluted tocomprise a desired composition of dissolved solids (e.g., ash) and/ortotal solids. In some embodiments, a volume of separated solution may bediluted to have a total solids content at a value of less than 0.5%w/w), less than 1% (w/w) or less than 2% (w/w), or less than 4% (w/w),or less than 6% (w/w) or less than 8% (w/w), or less than 10% (w/w).According to some embodiments, a separated solution may be diluted tohave a turbidity value (e.g., relative to absorbance of a 500 nm lightsource where 1.0 is equivalent to 10% absorbance and 10.0 is equivalentto 100% absorbance) of a volume of separated solution at a value of lessthan about 0.5, or less than about 0.75, or less than about 1.0, or lessthan about 1.25, or less than about 1.5, where about may represent plusor minus 5%. In some embodiments, a separated solution may be diluted tohave an electrical conductivity value of less than about 2000 μS/cm, orless than about 2500 μS/cm, or less than about 3000 μS/cm, or less thanabout 3500 μS/cm, or less than about 4000 μS/cm, or less than about 4500μS/cm, or less than about 5000 μS/cm, or less than about 5500 μS/cm, orless than about 6000 μS/cm, where “about” may represent plus or minus250 μS/cm.

In some embodiments, a separated solution may be diluted relative to abiomass feed rate. According to some embodiments, a separated solutionin collection tank may be diluted relative to a feed to dilution ratioof about 4:1, or about 3.5:1, or about 3:1, or about 2.5:1, or about2:1, or about 1.5:1, or about 1:1.

Diluting a separated solution may include subjecting a donor stream anda recipient stream to a heat exchanger. According to some embodiments, aheat exchanger (e.g., thermal energy exchange mechanisms) may decreasean overall energy input required for production of high-concentrationprotein product (e.g., protein flake) from a microcrop (e.g., Lemna).According to some embodiments, a heat exchanger may include a flowsystem wherein a stream of discard solution (i.e., a donor stream) and adilution solution stream (i.e., recipient stream) are adjacent such thatthermal energy exchange may occur. In some embodiments, a dilutionsolution stream (i.e., a recipient stream) may have a cooler temperatureand thereby a lower thermal energy than a donor stream (e.g., a discardsolution stream which retains heat from a blanching solution). Accordingto some embodiments, a heat exchanger may include a flow system (e.g., aseries of pipes composed of conductive material) such that a dilutionsolution stream (i.e., a recipient stream) may absorb at least somethermal energy from a discard solution stream (i.e., a donor stream). Insome embodiments, a heat exchanger may result in increasing atemperature of a dilution solution stream and/or a diluted separatedsolution.

According to some embodiments, a separated blanching solution may befiltered (e.g., FIG. 1A 128, FIG. 2A 228) to form a filtered blanchingsolution (e.g., FIG. 1A 130) and a blanching waste. Filtration mayinclude, according to some embodiments, coarse filtration (e.g., gravityfiltration, vibratory screen filtration), fine filtration (e.g.,microfiltration, ultrafiltration, nanofiltration, reverse osmosisfiltration), or any combination thereof. A filtered blanching solutionmay be recycled as a wash solution (e.g., FIG. 1C 130), as a growthmedium in the cultivation of a microcrop (e.g., FIG. 1A 130), as ablanching solution, or any combination thereof. In some embodiments, ablanching waste (e.g., retentate from a filtration method) may berecycled as part of a growth medium (e.g., as a nutrient source) in acultivation of a microcrop (e.g., FIG. 1A 126, FIG. 2A 226). At leastabout 40%, or at least about 50%, or at least about 60%, or at leastabout 70%, or at least about 80%, or at least about 90%, or at leastabout 95% of a blanching solution separated from the wet proteinconcentrate may be recycled for future use (e.g., recycled blanchingsolution used as a first, second, or third wash solution or furthercycles of blanching), according to some embodiments.

Cooling a Wet Protein Concentrate

According to some embodiments, a wet protein concentrate may be cooled(e.g., FIG. 1B 112). A cooling procedure may be performed by exposing(e.g., submerging, spraying) at least one surface of a wet proteinconcentrate to a cooling solution (e.g., water), or exposing at leastone surface of a wet protein concentrate to decreased air temperaturesor convective cooling conditions (e.g., wind, air movement), in someembodiments.

In some embodiments a cooling procedure may be performed by exposing(e.g., submerging, spraying) at least one surface of a wet proteinconcentrate to a cooling solution (e.g., water). A cooling solution, insome embodiments, may be combined with a wet protein concentrate (e.g.,first portion, second portion) to form a slurry. According to someembodiments, a cooling solution may be combined with a wet proteinconcentrate after separation from a blanching solution. According tosome embodiments, a blanching procedure may involve agitation orstirring of a blanching solution/biomass slurry. Agitation or stirringof a blanching solution/biomass slurry may be perpetual or intermittent,according to some embodiments. According to some embodiments, a dilutionsolution may be used to cool a wet protein concentrate, the dilutionsolution may then be collected and used to dilute a separated solution.

A cooling solution may remain in contact with a wet protein concentratefor at least about 30 seconds, or at least about 1 min, or at leastabout 5 min, or at least about 10 min, or at least about 15 min, or atleast about 20 min, or at least about 25 min, or at least about 30 min.Some or all of a cooling solution, in some embodiments, may be separatedfrom a wet protein concentrate (e.g., using an inclined screen orvibratory screen). A cooling solution may be separated from a wetprotein concentrate, in some embodiments, using gravity separation,draining, an inclined screen, a vibratory screen, filtration, a decantercentrifuge, a belt press, a fan press, a rotary press, a screw press, afilter press, a finisher press, or any combination thereof, according tosome embodiments.

In some embodiments, some or all of a cooling solution may be collectedand reused/recycled. At least about 40%, or at least about 50%, or atleast about 60%, or at least about 70%, or at least about 80%, or atleast about 90%, or at least about 95% of a cooling solution (e.g.,water) separated from the wet protein concentrate may be recycled forfuture use as a cooling solution, a wash solution, as a growth mediumfor cultivation of a microcrop, or any combination thereof, according tosome embodiments.

A cooling solution may have a temperature below room temperature (e.g.,about 12° C.) at the time of use. In some embodiments, a coolingsolution may have a temperature below about 50° C., or below about 40°C., or below about 30° C., or below about 20° C., or below about 15° C.,or below about 10° C., or below about 5° C., or below about 2° C., orbelow about 1° C., or below about 0° C. at the time of use. A coolingsolution may have a temperature between about 0° C. and about 10° C., orbetween about 5° C. and about 15° C., or between about 10° C. and about20° C., or 15° C. and about 25° C., or between about 20° C. and about30° C., or between about 0° C. and about 50° C. at the time of use, insome embodiments.

According to some embodiments, a wet protein concentrate may be cooledby exposing at least one surface of a wet protein concentrate todecreased air temperatures, or convective cooling conditions (e.g.,wind, air movement), or any combination thereof. In some embodiments, awet protein concentrate may be separated from a blanching solutionbefore exposure of the wet protein concentrate to decreased airtemperatures, or convective cooling conditions (e.g., wind, airmovement), or any combination thereof. A slurry of a wet proteinconcentrate and a blanching solution may be exposed to decreased airtemperatures, or convective cooling conditions (e.g., wind, airmovement), or any combination thereof, according to some embodiments.

A decreased air temperature, in some embodiments, may include atemperature of less than 30° C., or less than 25° C., or less than 20°C., or less than 15° C., or less than 10° C., or less than 5° C., orless than 2° C., or less than 1° C., or less than 0° C.

Reducing a Moisture Content of a Wet Protein Concentrate

In some embodiments a process may be used to reduce a moisture contentof a wet protein concentrate. According to some embodiments, a moisturecontent of a wet protein concentrate may be reduced without cooling thewet protein concentrate (e.g., FIG. 1B 112). Reducing a moisture contentof a wet protein concentrate may reduce capital and operationalexpenditures, for example, by reducing the energy needed to dry an endprotein product (e.g., protein concentrate flake/granule).

In some embodiments an evaporation process may be used to reduce amoisture content of a wet protein product. Evaporation may be performedby, for example, a thermal (evaporative) means such as: a rising filmevaporator, a falling film evaporator, a natural circulation evaporator(vertical or horizontal), an agitated-film evaporator, a multiple-effectevaporator, by vacuum evaporation, or any combination thereof. Heat maybe supplied directly into the evaporator, or indirectly through a heatjacket. Heat may either come from a raw source (e.g., combustion ofnatural gas, steam from a boiler) or from a waste heat stream (e.g.,dryer exhaust) or from heat transferred by cooling the input stream.

According to some embodiments, a moisture content of a wet proteinconcentrate may be reduced using gravity separation, draining, aninclined screen, a vibratory screen, filtration, a decanter centrifuge,a belt press, a fan press, a rotary press, a screw press, a filterpress, a finisher press, or any combination thereof.

In some embodiments an antioxidant (e.g., rosemary extract, Duralox®,Phyt-O-Blend CA) may be mixed with a wet protein product prior to dryingto improve shelf life of product (e.g., shelf life of a packagedproduct). According to some embodiments, lecithin may be mixed with awet protein product prior to drying to improve a mouth-feel of aproduct.

Solvent Extraction of Wet Protein Concentrate

According to some embodiments, processing a microcrop, or a biomass(e.g., first portion, second portion), or a wet protein concentrate mayinclude a solvent extraction procedure (e.g., FIG. 2A 232) to generate asolvent washed protein product.

A solvent washed protein product, in some embodiments, may haveincreased protein purity when compared to a protein product that was notsubjected to a solvent extraction procedure. A solvent extractionprocedure (e.g., FIG. 2A 232) may decolor a microcrop, or a biomass, ora wet protein concentrate, according to some embodiments, resulting in asolvent washed protein product having a reduced chlorophyll content(e.g., visually perceivable reduction in green coloration) compared tounwashed counterparts. In some embodiments, a solvent extractionprocedure may reduce a fat content of a protein concentrate (e.g., wet,flake/granule, flour). The reduction of a fat content may increase theshelf-life, improve odor, and/or improve a taste of a high-concentrationprotein product.

Solvent extraction of a microcrop, or a biomass, or a wet proteinconcentrate, in some embodiments, may comprise exposing (e.g.,submerging, spraying, dripping) at least one surface of the microcrop,or the biomass, or the wet protein concentrate to a solvent solution(e.g., ethanol, methanol, acetone). A solvent solution, in someembodiments, may be combined with a microcrop, or a biomass, or a wetprotein concentrate (e.g., first portion, second portion) to form aslurry. According to some embodiments, a solvent extraction proceduremay include exposing (e.g., submerging, spraying, dripping, slurry) atleast one surface of a microcrop, or a biomass, or a wet proteinconcentrate to a solvent solution for at least about 5 sec., at leastabout 15 sec., at least about 30 sec., at least about 45 sec., at leastabout 1 min., at least about 2 min., at least about 3 min., at leastabout 5 min., at least about 10 min., at least about 20 min., at leastabout 30 min., at least about 40 min., at least about 50 min., at leastabout 1 hour, at least about 2 hours, at least about 3 hours, at leastabout 4 hours, at least about 5 hours, at least about 6 hours, at leastabout 12 hours, or at least about 24 hours. A solvent extractionprocedure, in some embodiments, may include moving (e.g., agitating,stirring, propelling) at least a portion of a solvent solution at aspecified time, intermittently, or continually.

In some embodiments a solvent solution may include one or more alcohols(e.g., ethanol, methanol, propanol, isopropanol, glycerol), acetone,dichloromethane, ethyl acetate, hexane, ketones, or combinationsthereof. A solvent solution may comprise at least about 10% (v/v), atleast about 20% (v/v), at least about 30% (v/v), at least about 40%(v/v), at least about 50% (v/v), at least about 60% (v/v), at leastabout 70% (v/v), at least about 80% (v/v), or at least about 90% (v/v)of one or more alcohols (e.g., ethanol, methanol, propanol, isopropanol,glycerol), acetone, dichloromethane, ethyl acetate, hexane, ketones, orcombinations thereof.

In some embodiments, a solvent may be recovered (e.g., FIG. 2A 234) andrecycled (e.g., FIG. 2A 238). Furthermore, according to someembodiments, a chlorophyll byproduct and/or a fat byproduct (e.g., FIG.2A 236) extracted from a wet protein concentrate by solvent extraction(e.g., FIG. 2A 232) may be recovered from the solvent (e.g., FIG. 2A234).

A solvent washed protein product, in some embodiments, may have areduced fat content (e.g., about 2% of a protein concentrateflake/granule or less by weight) and/or a reduced chlorophyll content(e.g., visually perceivable reduction in green coloration) compared tounwashed counterparts. In some embodiments, a solvent washed proteinproduct may appear colorless, white, substantially white, or havereduced green coloration. A solvent washed protein product, in someembodiments, may exhibit at least one of an improved odor, taste, color,shelf life (e.g., reduced oxidation of fats), protein density,malleability, or combinations thereof.

In some embodiments, a solvent washed protein product may have a fatcontent comprising (w/w) lower than about 20%, or lower than about 15%,or lower than about 10%, or lower than about 5%, or lower than about 4%,or lower than about 3%, or lower than about 2%, or lower than about 1%,or lower than 0.5%, or lower than 0.4%, or lower than 0.3%, or lowerthan 0.2%, or lower than 0.1% by weight of a dry protein concentrate(e.g., flake, granule, flour). According to some embodiments, a solventwashed protein product may have a fat content comprising from about 0.1%to about 10%, or from about 0.1% to about 5%, or from about 0.1% toabout 2%, or from about 0.1% to about 1%, or from about 0.1% to about0.5% by weight of the a dry protein concentrate (e.g., flake, granule,flour).

Drying a Protein Product

A wet protein concentrate or a solvent washed protein product may bedried to generate a protein concentrate flake or a protein concentrategranule (e.g., first portion, second portion), according to someembodiments. A drying procedure, in some embodiments, may reduce amoisture content of a wet protein concentrate or a solvent washedprotein product to a desired level (e.g., lower moisture content, adesired moisture content). A moisture content of a protein concentrateflake/granule may be, for example, below about 90%, or below about 80%,or below about 70%, or below about 60%, or below about 50%, or belowabout 40%, or below about 30%, or below about 20%, or below about 10%,or below about 5%, or below about 1% by weight of the proteinconcentrate flake/granule, in some embodiments. A drying procedure maybe performed using a mechanism including, for example, a spray dryer, adrum dryer, a double drum dryer, flash dryer, a fluid-bed dryer, aconvection dryer, an evaporator, or any combination thereof.

In some embodiments, an inlet temperature of a dryer mechanism (thetemperature at the entrance to a dryer) may be above 25° C., or above50° C., or above 75° C., or above 100° C., or above 125° C., or above150° C., or above 175° C., or above 200° C., or above 225° C., or above250° C., or above 275° C., or above 300° C., or above 325° C., or above350° C., or above 375° C., or above 400° C., or above 425° C., or above450° C., or above 475° C., or above 500° C. An inlet temperature, insome embodiments, may be from about 25° C. to about 50° C., or fromabout 50° C. to about 75° C., or from about 75° C. to about 100° C., orfrom about 100° C. to about 125° C., or from about 125° C. to about 150°C., or from about 150° C. to about 175° C., or from about 175° C. toabout 200° C., or from about 200° C. to about 225° C., or from about225° C. to about 250° C., or from about 250° C. to about 275° C., orfrom about 275° C. to about 300° C., or from about 300° C. to about 325°C., or from about 325° C. to about 350° C., or from about 350° C. toabout 375° C., or from about 375° C. to about 400° C., or from about400° C. to about 425° C., or from about 425° C. to about 450° C., orfrom about 450° C. to about 475° C., or from about 475° C. to about 500°C., or above 500° C. An inlet temperature may be from about 50° C. toabout 100° C., or from about 100° C. to about 150° C., or from about150° C. to about 200° C., or from about 200° C. to about 250° C., orfrom about 250° C. to about 300° C., or from about 300° C. to about 350°C., or from about 350° C. to about 400° C., or from about 400° C. toabout 450° C., or from about 450° C. to about 500° C., or above 500° C.,in some embodiments. According to some embodiments, an inlet temperatureof a dryer mechanism may be about 225° C.

According to some embodiments, an outlet temperature of a dryermechanism (the temperature at the exit from a dryer) may be below about300° C., or below about 275° C., or below about 250° C., or below about225° C., or below about 200° C., or below about 175° C., or below about150° C., or below about 125° C., or below about 100° C., or below about75° C., or below about 50° C., or below about 25° C. An outlettemperature may be from about 300° C. to about 275° C., or from about275° C. to about 250° C., or from about 250° C. to about 225° C., orfrom about 225° C. to about 200° C., or from about 200° C. to about 175°C., or from about 175° C. to about 150° C., or from about 150° C. toabout 125° C., or from about 125° C. to about 100° C., or from about100° C. to about 75° C., or from about 75° C. to about 50° C., or fromabout 50° C. to about 25° C., or below about 25° C., in someembodiments. An outlet temperature, in some embodiments, may be fromabout 300° C. to about 250° C., or from about 250° C. to about 200° C.,or from about 200° C. to about 150° C., or from about 150° C. to about100° C., from about 100° C. to about 50° C., or from about 50° C. toabout 25° C., or below about 25° C. According to some embodiments, anoutlet temperature of a dryer mechanism may be about 75° C.

In some embodiments, a volume of a wet protein concentrate or a volumeof a solvent washed protein product may be mixed with a volume of aprotein concentrate flake/granule prior to drying. This process, knownas back-mixing, may be employed when, for example, the moisture contentof a wet protein concentrate exceeds the level that a dryer mechanism iscapable of accepting. By back-mixing a protein concentrate flake/granulewith a wet protein concentrate or a solvent washed protein product, atotal moisture content may be kept within the specifications of a dryermechanism, thereby reducing operational costs (e.g., wear and tear onequipment).

Milling

According to some embodiments, a protein concentrate flake/granule maybe milled (e.g., FIG. 1A 118, FIG. 2A 218) to form a protein concentrateflour 120. A milling procedure may involve a hammer mill, a pin mill, avibrating mill, a fluid energy mill, a jet mill or any combinationthereof.

An antioxidant (e.g., rosemary extract, Duralox®, Phyt-O-Blend CA) maybe mixed with a protein concentrate flake/granule or a proteinconcentrate flour before packaging, according to some embodiments.

According to some embodiments, a wet protein concentrate or a partiallydried (e.g., having a reduced moisture content) wet protein concentrateor a solvent washed protein concentrate may be frozen, flash-frozen, orfreeze dried.

In some embodiments, a wet protein concentrate or a solvent washedprotein concentrate may be milled prior to drying (e.g., a dry milledprotein concentrate).

Protein Concentrate

Some embodiments relate to a process for production of ahigh-concentration protein product (e.g., a wet protein concentrate, asolvent washed protein concentrate, a protein concentrate flake/granule,a protein concentrate flour, a dry milled protein concentrate) from abiomass of a harvested microcrop (e.g., aquatic plant species, Lemna,algal species). A process may be configured or performed to achieve anydesired protein yield (e.g., maximal yield, a selected yield). In someembodiments, a high-concentration protein product may have a proteinconcentration of at least about 35%, or at least about 40%, or at leastabout 45%, or at least about 50%, or at least about 60%, or at leastabout 65%, or at least about 70%, or at least about 75%, or at leastabout 80% by dry mass basis (DMB). A remainder of a high-concentrationprotein product may include carbohydrates, fiber, fats, minerals, or anycombination thereof. A high-concentration protein product proteinconcentrate may be suitable for animal feed and/or human consumption.For example, a high-concentration protein product may serve as aneffective replacement for protein concentrates (e.g., soy, pea) whichare presently used in a large number of human food products eitherindividually or as ingredients and additives. According to someembodiments, at least of portion of a protein composition of ahigh-concentration protein product may comprise denatured orpartially-denatured protein.

Protein Digestibility Corrected Amino Acid Score (PDCAAS) andDigestibility

According to some embodiments, a high-concentration protein product mayhave a PDCAAS relative to a reference standard (e.g., casein) of atleast 0.88, or at least 0.89, or at least 0.90, or at least 0.91, or atleast 0.92, or at least 0.93, or at least 0.94, or at least 0.95. Insome embodiments, a high-concentration protein product may have a PDCAASof between 0.88 and 0.94, or between 0.90 and 0.94, or between 0.92 and0.94. PDCAAS may be evaluated, for example, by an animal (e.g., rat)model or by an in vitro enzyme digestion model. Calculating a PDCAASvalue may be dependent upon a limiting amino acid. According to someembodiments, a PDCAAS value of a high-concentration protein product maybe limited by a histidine composition.

In some embodiments, a high-concentration protein product may have adigestibility of at least 88%, or at least 90%, or at least 92%, or atleast 94%, or at least 95%, or at least 96%, or at least 97%, or atleast 98% in each case. Digestibility may be determined, for example,using a rat model (casein digestibility) or an in vitro digestibilitymethod (e.g., Animal-Safe Accurate Protein Quality Score (ASAP-QualityScore) method, TIM model, dynamic gastric model (DGM)).

Amino Acid Composition

In some embodiments, a high-concentration protein product may compriseone or more essential amino acids. For example, a high-concentrationprotein product may include one or more amino acids selected fromleucine, isoleucine, lysine, methionine, phenylalanine, threonine,tryptophan, valine, histidine, arginine, aspartic acid, serine, glutamicacid, proline, glycine, alanine, tyrosine and cysteine. Theconcentration of an essential amino acid may be at least about 1 g/100 gof protein concentrate, or at least about 1.5 g/100 g of proteinconcentrate, or at least about 2 g/100 g of protein concentrate, or atleast about 2.5 g/100 g of protein concentrate, or at least about 3g/100 g of protein concentrate, or at least about 4 g/100 g of dry atleast about 2.5 g/100 g of protein concentrate, or at least about 3g/100 g of protein concentrate, or at least about 4 g/100 g of proteinconcentrate, or at least about 5 g/100 g of protein concentrate, or atleast about 6 g/100 g of protein concentrate, or at least about 7 g/100g of protein concentrate, or at least about 8 g/100 g of proteinconcentrate, or at least about 9 g/100 g of protein concentrate, or atleast about 10 g/100 g of protein concentrate in some embodiments.

The concentration of an amino acid (e.g., an essential amino acid), insome embodiments, may be expressed as a weight fraction of the proteinrecovered from a high-concentration protein product, and is at leastabout 1 g/100 g of protein, or at least about 1.5 g/100 g of protein, orat least about 2 g/100 g of protein, or at least about 2.5 g/100 g ofprotein, or at least about 3 g/100 g of protein, or at least about 4g/100 g of protein, or at least about 5 g/100 g of protein, or at leastabout 6 g/100 g of protein, or at least about 7 g/100 g of protein, orat least about 8 g/100 g of protein, or at least about 9 g/100 g ofprotein, or at least about 10 g/100 g of protein.

For example, a high-concentration protein product produced by theprocesses described herein may include the amino acid contentssummarized in Table 2 below.

TABLE 2 Amino Acid Profiles of High Concentration Protein Products(g/100 g protein) Amino Acid Product 1 Product 2 Tryptophan 2.1 2.1 +10% Alanine 4.8 4.8 + 10% Arginine 5.7 5.7 + 10% Aspartic Acid 7.8 7.8 +10% Glutamic Acid 9.4 9.4 + 10% Glycine 4.1 4.1 + 10% Histidine 2.02.0 + 10% Isoleucine 4.4 4.4 + 10% Leucine 7.7 7.7 + 10% Phenylalanine +8.8 8.8 + 10% Tyrosine Proline 3.9 3.9 + 10% Serine 3.4 3.4 + 10%Threonine 3.7 3.7 + 10% Lysine 6.0 6.0 + 10% Valine 5.3 5.3 + 10%Cysteine + 2.9 2.9 + 10% Methionine

Fat Content

In some embodiments, a high-concentration protein product may have a fatcontent lower than about 20%, or lower than about 15%, or lower thanabout 10%, or lower than about 8%, or lower than about 5%, or lower thanabout 4%, or lower than about 3%, or lower than about 2%, or lower thanabout 1%, or lower than 0.5%, or lower than 0.4%, or lower than 0.3%, orlower than 0.2%, or lower than 0.1% by DMB of the protein product. Ahigh-concentration protein product may have a fat content from about 1%to about 10%, or from about 10% to about 20%, or from about 0.1% toabout 10%, or from about 0.1% to about 5%, or from about 0.1% to about2%, or from about 0.1% to about 1%, or from about 0.1% to about 0.5% byDMB of the high-concentration protein product in some embodiments. Aprotein concentrate may be further processed to meet a desired fatcontent (e.g., higher or lower concentration, a desired fatcomposition).

Chlorophyll Content

According to some embodiments, a high-concentration protein product mayhave a reduced chlorophyll content. In some embodiments, ahigh-concentration protein product may appear colorless or have reducedgreen coloration. A high-concentration protein product may have achlorophyll content of less than 6,000 mg/100 g, or less than 5,500mg/100 g, or less than 5,000 mg/100 g, or less than 4,500 mg/100 g, orless than 4,000 mg/100 g, or less than 3,500 mg/100 g, or less than3,000 mg/100 g.

Apiogalacturonan and/or Oligogalacturan Content

In some embodiments, a high-concentration protein product may include atleast one apiogalacturonan and/or oligogalacturonide. According to someembodiments, a high-concentration protein product polysaccharide productmay have a concentration of at least one apiogalacturonan of at least 1%DMB, or at least 3% DMB, or at least 5% DMB, or at least 7% DMB, or atleast 10% DMB, or at least 12% DMB, or at least 15% DMB, or at least 20%DMB, or at least 25% DMB, or at least 30% DMB. A high-concentrationprotein product, in some embodiments, may have a concentration of atleast one apiogalacturonan of at least 10% DMB. In some embodiments, apolysaccharide product may have a concentration of at least oneapiogalacturonan of at least 15% DMB. Concentrations recited in thisparagraph may refer to a single apiogalacturonan or to the combined(total) concentration of two or more (up to all) apiogalacturonanspresent, according to some embodiments.

According to some embodiments, a concentration of at least oneapiogalacturonan and/or oligogalacturonide in a high-concentrationprotein product may be determined by a phenol-sulfuric acid method, suchas that described in Dubois, M., Gilles, K. A., Hamilton, J. K., et al.,Anal. Chem., 1956, vol. 28, no. 2, 350-356. A concentration of at leastone apiogalacturonan and/or oligogalacturonide in a high-concentrationprotein product may be determined using UV spectrophotometry, such asthat described in Albalasmeh, A., Berhe, A., and Ghezzeher, T.,Carbohydrate Polymers, 2013, vol. 97, no. 2, 253-261, in someembodiments. Any desired method may be used to determine a concentrationof at least one apiogalacturonan and/or oligogalacturonide in ahigh-concentration protein product.

A monosaccharide composition of a concentration of a high-concentrationprotein product may be determined by high pressure anion exchangechromatography (HPAEC), according to some embodiments. For example,HPAEC may be performed using a Dionex CarboPac PA1 column withamperometric detection of polysaccharide hydrolysis where hydrolysis wasperformed under the following conditions: (1) hydrolysis with 2NTrifluoracetic acid (TFA) at 100° C. for 0.5 hours; (2) hydrolysis with2N TFA at 100° C. for 4 hours; (3) hydrolysis with 2N H₂SO₄ at 100° C.for 6 hours; (4) hydrolysis with 2N H₂SO₄ at 100° C. for 6 hours afterovernight exposure to 26N H₂SO₄ at room temperature.

In some embodiments, a monosaccharide composition of ahigh-concentration protein product may be determined by gas phasechromatography. For example, the relative composition of amonosaccharide of a high-concentration protein product may be identifiedand quantified by (1) hydrolyzing the product to form monosaccharides bymethaolysis; (2) trimethylsilying the monosaccharides to formvolatilized monosaccharides; and (3) quantifying and identifying thevolatilized monosaccharides as O-methylglycosides by gas phasechromatography.

Oxalic Acid Content

According to some embodiments, a high-concentration protein product mayhave a reduced oxalic acid (H₂C₂O₄ or HOOCCOOH) content. In someembodiments, a high-concentration protein product may have an oxalicacid content of lower than about 1.5%, or lower than about 1.4%, orlower than about 1.3%, or lower than about 1.2%, or lower than about1.1%, or lower than about 1.0%, or lower than about 0.9%, or lower thanabout 0.8%, or lower than about 0.75%, or lower than about 0.7%, orlower than about 0.65%, or lower than about 0.6%, lower than about0.55%, lower than about 0.5%, or lower than about 0.45%, or lower thanabout 0.4%, or lower than about 0.35%, or lower than about 0.3%, orlower than about 0.25%, or lower than about 0.2%, or lower than about0.15%, or lower than about 0.1%, or lower than about 0.05%, or lowerthan about 0.04%, or lower than about 0.03%, or lower 0.02% by DMB. Ahigh-concentration protein product, in some embodiments may have anoxalic acid content of from about 0.02% to about 0.6%, from about 0.02%to about 0.5%, or from about 0.02% to about 0.4%, or from about 0.02% toabout 0.3%, or from about 0.02% to about 0.2%, or from about 0.02% toabout 0.15%, or from about 0.02% to about 0.1% by DMB. In someembodiments, a high-concentration protein product may have an oxalicacid content of no more than 0.1%. According to some embodiments, ahigh-concentration protein product may have an oxalic acid content of nomore than 0.05% DMB.

Polyphenol Content

In some embodiments, a high-concentration protein product may be reducedin at least one polyphenol (e.g., tannin). In some embodiments, ahigh-concentration protein product (e.g., a wet protein concentrate, asolvent washed protein concentrate, a protein concentrate flake/granule,a protein concentrate flour), may comprise polyphenol (e.g., totalsoluble polyphenol) at a concentration (mg/100 g of high-concentrationprotein product) of less than about 1.5 mg/100 g, or less than about1.55 mg/100 g, or less than about 1.6 mg/100 g, or less than about 1.65mg/100 g, or less than about 1.7 mg/100 g, or less than about 1.75mg/100 g, or less than about 1.8 mg/100 g, or less than about 1.85mg/100 g, or less than about 1.9 mg/100 g, or less than about 2.0 mg/100g, or less than about 2.2 mg/100 g, or less than about 2.4 mg/100 g, orless than about 2.6 mg/100 g, or less than about 2.8 mg/100 g, or lessthan about 3.0 mg/100 g, or less than about 3.2 mg/100 g.

Ash Content

According to some embodiments, a high-concentration protein product mayinclude an ash content consisting of a residue containing inorganicmineral elements. An ash content in some embodiments may be determinedby combusting a protein product at a high temperature (e.g., ≥500° C.)to remove organic matter. A high-concentration protein product may havean ash content lower than about 50%, or lower than about 40%, or lowerthan about 30%, or lower than about 25%, or lower than about 20%, orlower than about 15%, or lower than about 10%, or lower than about 5%,or lower than about 4%, or lower than about 3%, or lower than about 2%,or lower than about 1% by DMB of the protein product, in someembodiments. A high-concentration protein concentrate may be furtherprocessed to meet a desired ash content (e.g., higher or lowerconcentration, a desired ash composition), according to someembodiments.

Carbohydrate Content

According to some embodiments, a high-concentration protein product mayhave a carbohydrate content (e.g., pectin) lower than about 50%, orlower than about 40%, or lower than about 30%, or lower than about 25%,or lower than about 20%, or lower than about 15%, or lower than about10%, or lower than about 5%, or lower than about 4%, or lower than about3%, or lower than about 2%, or lower than about 1% by DMB of the proteinproduct. A high-concentration protein product, in some embodiments, mayhave a carbohydrate content from about 1% to about 10%, or from about10% to about 20%, or from about 20% to about 30%, or from about 30% toabout 40%, or from about 40% to about 50% by DMB of the protein product.In some embodiments, a high-concentration protein product may have acarbohydrate content from about 1% to about 50%, or from about 2% toabout 40%, or from about 5% to about 30%, or from about 8% to about 20%,or from about 10% to about 15% by DMB of the protein product. Ahigh-concentration protein product may be further processed to meet adesired carbohydrate content (e.g., higher or lower concentration, adesired carbohydrate composition).

Dietary Fiber Content

In some embodiments, a high-concentration protein product may have adietary fiber content of at least about 20% DMB, or at least about 25%,or at least about 30%, or at least about 35%, or at least about 40%, orat least about 45%, or at least about 50%, where “about” may representplus or minus 3%. According to some embodiments, a high-concentrationprotein product may have a dietary fiber content between about 20% andabout 45%, or between about 30% and about 45%, or between about 35% andabout 45%, where “about” may represent plus or minus 3%. Ahigh-concentration protein product may be further processed to meet adesired dietary fiber content (e.g., higher or lower concentration, adesired dietary fiber composition).

Water-Binding Capacity

In some embodiments, a high-concentration protein product may have awater-binding capacity of about 4 milliliters of water per gram ofhigh-concentration protein product (mug), or about 4.5 ml/g, or about5.0 ml/g, or about 6.0 ml/g, or about 7.0 ml/g, or about 7.5 ml/g, orabout 8.0 ml/g, or about 8.5 ml/g, or about 9.0 ml/g, or about 9.5 ml/g,or about 10.0 ml/g. According to some embodiments, a high-concentrationprotein product may have a water binding capacity of at least 4 ml/g, orat least 5 ml/g, or at least 6 ml/g, or at least 7 ml/g, or at least 7.5ml/g, or at least 8 ml/g, or at least 8.5 ml/g, or at least 9 ml/g, orat least 9.5 ml/g.

Oil-Binding Capacity

In some embodiments, a high-concentration protein product may have anoil-binding capacity (e.g., corn oil) of about 2 milliliters of oil(e.g., corn oil) per gram of high-concentration protein product (ml/g),or about 2.5 ml/g, or about 3.0 ml/g, or about 3.5 ml/g, or about 4.0ml/g, or about 4.5 ml/g, or about 5.0 ml/g, or about 5.5 ml/g. Accordingto some embodiments, a high-concentration protein product may have awater binding capacity of at least 2 ml/g, or at least 2.5 ml/g, or atleast 3.0 ml/g, or at least 3.5 ml/g, or at least 4.0 ml/g, or at least4.5 ml/g, or at least 5.0 ml/g, or at least 5.5 ml/g. For example, ahigh-concentration protein product produced by the processes describedherein may include the contents summarized in Table 3 below.

TABLE 3 Example Compositions of High-Concentration Protein ProductsCharacteristic Product 1 Product 2 Product 3 Product 4 Solids (DMB) ≥9088-95 ≥90 88-95 Moisture (DMB) ≤10  5-12 ≤10  5-12 Protein (DMB) ≥5050-65 ≥45 35-45 PDCASS ≥0.90 0.88-0.94 ≥0.90 0.88-0.94 PDCASS LimitingHistidine Histidine Histidine Histidine Amino Acid Digestibility ≥0.900.85-0.96 ≥0.90 0.85-0.96 Fat (DMB) ≤1 0.05-1.5  ≤10  5-10 Ash (DMB) ≤10 5-15 ≤10  5-15 Dietary Fiber (DMB) ≥40 35-45 ≥40 35-45 Othercarbohydrates ≤5  1-10 ≤5  5-10 (DMB) Oxalic acid ≤1.5 0.2-2.5 ≤10.2-2.0

Any desired method may be used to determine a composition of ahigh-concentration protein product.

A product and/or process, in some embodiments, may be configured orperformed so other characteristics of a high-concentration proteinproduct (e.g., particle size, bacterial specification) meet desiredcriteria and/or may be suitable for an intended purpose.

In some embodiments, a high-concentration protein product may be packedand/or sealed in either an industry standard bag or drum of varyingsizes. A sealing method of industry-standard grade may be used to ensureproper shelf-life and shipping conditions. A bag or drum may includeprinted instructions or specifications regarding, for example, itsintended use, shelf-life, suggested storage conditions, shippingconditions, compositions, or the like, or a combination thereof. Anantioxidant (e.g., rosemary extract, Duralox®, Phyt-O-Blend CA) may bemixed with a protein product before drying or packaging, according tosome embodiments. According to some embodiments, lecithin may be mixedwith a wet protein product prior to drying to improve a mouth-feel of aproduct.

FIGS. 1A, 1B, 1C, and 1D

FIGS. 1A, 1B, 1C, and 1D are schematic diagrams illustrating a method100 for growing, harvesting, and processing a microcrop (e.g., aquaticplant species, Lemna, algal species) for the production of ahigh-concentration protein product according to a specific exampleembodiment of the disclosure. A microcrop (e.g., Lemna) may becultivated in a bioreactor system 102 and harvested 104 to form abiomass. As shown in FIGS. 1A through 1D, in some embodiments a biomassmay be processed to form a high-concentration protein product includinga wet protein concentrate 111, a protein concentrate flake/granule 118,protein concentrate flour 122, or any combination thereof.High-concentration protein products may include products suitable foranimal feed and/or human consumption. A process 100 may be performedindoors, outdoors, and any combination thereof based, for example, onthe specific environmental characteristics of the location(s).

As shown in FIGS. 1A through 1D, a microcrop may be cultivated in abioreactor system 102 (e.g., open bioreactor, closed bioreactor). Abioreactor system may contain a growth medium (e.g., water, a nutrientcomposition). In some embodiments, a bioreactor system, in someembodiments, may be configured to collect rainfall and/or to intakewater from a source of recycled or ground water (e.g., storm water,recycled water) or any other suitable source. A bioreactor system may beconfigured, in some embodiments, to insert additional nutrients (e.g.,nitrogen, phosphorus, potassium) or gases (e.g., oxygen; carbon dioxide)at desired time indicators or in response to sensor readings. In someembodiments, a bioreactor system may comprise a monitoring system. Abioreactor system, in some embodiments, may monitor and adjust athickness and distribution of a microcrop mat. For example, when amicrocrop reaches a desired thickness or distribution a bioreactorsystem may initiate harvest procedures.

At specified times (e.g., based on environmental conditions) or after amicrocrop develops desired characteristics (e.g., mat thickness; matdistribution; maturation), a microcrop may be harvested 104 (e.g.,manual, automated) from a bioreactor system, forming a biomass 105. Anautomated skimmer system, in some embodiments, may collect a microcropfrom a bioreactor system and transfer a harvested microcrop (e.g., via apumping system) onto an inclined vibrating screen to separate a biomassfrom growth medium and debris. In some embodiments a microcrop may beharvested by vacuum skimming the microcrop from a bioreactor systemthrough a stationary screen filter. A microcrop may be harvestedmanually, according to some embodiments. A biomass slurry, including aharvested microcrop (e.g., Lemna) and a growth medium (e.g., water), maybe conveyed to an inclined screen, which may optionally vibrate, where abiomass (e.g., microcrop) may be separated from the growth medium.

During harvesting 104, a separated growth medium may be recycled backinto the bioreactor system or to an additional storage container (e.g.,container or pond), according to some embodiments. In some embodiments,at least about 40% (v/v), or at least about 50% (v/v), or at least about60% (v/v), or at least about 70% (v/v), or at least about 80% (v/v), orat least about 90% (v/v), or at least about 95% (v/v) of a growth medium(e.g., water) separated from a biomass may be recycled for future use.

As shown in FIGS. 1C and 1D, a biomass 105 may go through a washprocedure 106 (e.g., submerging, spraying, slurry) to remove debris,contaminants, microorganisms, and/or toxins. In some embodiments a washprocedure may be performed by exposing (e.g., submerging, spraying) atleast about one surface of a biomass to a wash solution (e.g., water,growth medium, antimicrobial solution). A wash solution (e.g., water,ozonated water), in some embodiments, may be combined with a biomass toform a slurry. According to some embodiments, multiple washes (e.g., afirst wash solution, a second wash solution, a third wash solution) maybe applied to a biomass. Some or all of a wash solution (e.g., a first,second, and/or third wash solution), in some embodiments, may beseparated from a biomass (e.g., using an inclined screen or vibratoryscreen).

In some embodiments, some or all of a wash solution, second washsolution, and/or third wash solution may be collected andreused/recycled 108. By volume, at least about 40%, or at least about50%, or at least about 60%, or at least about 70%, or at least about80%, or at least about 90%, or at least about 95% of a wash solution,second wash solution, and/or third wash solution (e.g., water) separatedfrom the biomass may be recycled for future use (e.g., recycled washsolution or used as growth medium in the bioreactor system 108),according to some embodiments.

As shown in FIGS. 1A through 1D, a biomass, either washed or unwashed,may be blanched 110 to form a wet protein concentrate 111. According tosome embodiments, a blanching procedure may include immersing orsubmerging a biomass in a blanching solution at a ratio of a blanchingsolution to a biomass (w/w) of 10:1, or 9:1, or 8:1, or 7:1, or 6:1, or5.5:1, or 5:1, or 4.5:1, or 4:1, or 3.5:1, or 3:1, or 2.5:1, or 2:1, or1.5:1, or 1:1. A blanching solution may comprise water, surface water,well water, distilled water, reverse osmosis, nanofiltered water, and/orrecycled fluid, according to some embodiments. In some embodiments, ablanching solution may further comprise at least one calcium salt (e.g.,calcium chloride, calcium acetate). A biomass may be blanched (e.g.,immersed/submerged in a blanching solution) having a temperature aboveabout 70° C., or above about 75° C., or above about 80° C., or aboveabout 85° C., or above about 90° C., or above about 95° C., or aboveabout 100° C. at the time of use for about 20 sec to about 40 sec, orabout 30 sec to about 45 sec, or about 30 sec to about 1 min, or about30 sec to about 1 min 30 sec, or about 30 sec to about 2 min, or about30 sec to about 5 min, or about 1 min to about 5 min, or about 1 min toabout 5 min, or about 1 min to about 10 min, or about 30 sec to about 10min, where “about” may represent plus or minus 10%, according to someembodiments. According to some embodiments, a biomass may be blanched atabout 85° C. for about 45 sec.

Some or all of a blanching solution may be separated from a wet proteinconcentrate 111 for example using gravity separation, draining, aninclined screen, a vibratory screen, filtration, a decanter centrifuge,a belt press, a fan press, a rotary press, a screw press, a filterpress, a finisher press, or any combination thereof. As shown in FIGS.1A through 1D, a separated blanching solution may be collected andreused/recycled 122. Further, according to some embodiments, a separatedblanching solution may be filtered 128 to form a filtered blanchingsolution 130 and a blanching waste. Filtration may include, according tosome embodiments, coarse filtration (e.g., gravity filtration, vibratoryscreen filtration), fine filtration (e.g., microfiltration,ultrafiltration, nanofiltration, reverse osmosis filtration), or anycombination thereof. As shown in FIGS. 1A through 1D, a filteredblanching solution may be recycled as a wash solution 130, as a growthmedium in the cultivation of a microcrop 130, as a blanching solution(not shown), or any combination thereof. In some embodiments, ablanching waste (e.g., retentate from a filtration method) may berecycled as part of a growth medium (e.g., as a nutrient source) in acultivation of a microcrop 126.

As shown in FIGS. 1B and 1D, a wet protein concentrate may be cooled112, for example by exposing (e.g., submerging, spraying) at least onesurface of a wet protein concentrate to a cooling solution (e.g., water)or exposing at least one surface of a wet protein concentrate todecreased air temperatures or convective cooling conditions (e.g., wind,air movement), in some embodiments. A cooling solution may have atemperature below room temperature (e.g., about 12° C.) at the time ofuse. A cooling solution, in some embodiments, may be combined with a wetprotein concentrate (e.g., first portion, second portion) to form aslurry. A cooling solution may remain in contact with a wet proteinconcentrate for at least about 30 seconds, or at least about 1 min, orat least about 5 min, or at least about 10 min, or at least about 15min, or at least about 20 min, or at least about 25 min, or at leastabout 30 min. Some or all of a cooling solution, in some embodiments,may be separated from a wet protein concentrate (e.g., using an inclinedscreen or vibratory screen).

As shown in FIGS. 1A through 1D, a wet protein concentrate may be dried114 to generate a protein concentrate flake or a protein concentrategranule 116 (e.g., first portion, second portion), according to someembodiments. A drying procedure may be performed using a mechanismincluding, for example, a spray dryer, a drum dryer, a double drumdryer, flash dryer, a fluid-bed dryer, a convection dryer, anevaporator, or any combination thereof.

According to some embodiments, a protein concentrate flake/granule maybe milled 118, as shown in FIGS. 1B and 1C, to form a proteinconcentrate flour. A milling procedure may involve a knife mill, ahammer mill, a pin mill, a vibrating mill, a jet mill, a fluid energymill, or any combination thereof.

FIGS. 2A, 2B, 2C, and 2D

FIGS. 2A, 2B, 2C, and 2D are schematic diagrams illustrating methods 200for growing, harvesting, and processing a microcrop (e.g., aquatic plantspecies, Lemna, algal species) for the production of ahigh-concentration protein product according to a specific exampleembodiment of the disclosure. A microcrop (e.g., Lemna) may becultivated in a bioreactor system 202 and harvested 204 to form abiomass 205. As shown in FIGS. 2A through 2D, in some embodiments abiomass may be processed to form a high-concentration protein productincluding a wet protein concentrate 211, a protein concentrateflake/granule 216, protein concentrate flour 220, or any combinationthereof and a chlorophyll and/or fat byproduct 228. High-concentrationprotein products may include products suitable for animal feed and/orhuman consumption. A process 200 may be performed indoors, outdoors, andany combination thereof based, for example, on the specificenvironmental characteristics of the location(s).

As shown in FIGS. 2A through 2D, a microcrop may be cultivated 202 in abioreactor system (e.g., open bioreactor, closed bioreactor) containinga growth medium (e.g., water, a nutrient composition). In someembodiments, a bioreactor system, may be configured to collect rainfalland/or to intake water from a source of recycled or ground water (e.g.,storm water, recycled water) or any other suitable source. A bioreactorsystem may be configured, in some embodiments, to insert additionalnutrients (e.g., nitrogen, phosphorus, potassium) or gases (e.g.,oxygen; carbon dioxide) at desired time indicators or in response tosensor readings. In some embodiments, a bioreactor system may comprise amonitoring system. A bioreactor system, in some embodiments, may monitorand adjust a thickness and distribution of a microcrop mat. For example,when a microcrop reaches a desired thickness or distribution abioreactor system may initiate harvest procedures.

At specified times (e.g., based on environmental conditions) or after amicrocrop develops desired characteristics (e.g., mat thickness; matdistribution; maturation), a microcrop may be harvested 204 (e.g.,manual, automated) from a bioreactor system, forming a biomass 205. Abiomass slurry, including a harvested microcrop (e.g., Lemna) and agrowth medium (e.g., water), may be conveyed to an inclined screen,which may optionally vibrate, where a biomass (e.g., microcrop) may beseparated from the growth medium.

As shown in FIGS. 2C and 2D, a biomass 205 may go through a washprocedure 206 (e.g., submerging, spraying, slurry) to remove debris,contaminants, microorganisms, and/or toxins. In some embodiments a washprocedure may be performed by exposing (e.g., submerging, spraying) atleast about one surface of a biomass to a wash solution (e.g., water,growth medium, antimicrobial solution). A wash solution (e.g., water,ozonated water), in some embodiments, may be combined with a biomass toform a slurry. According to some embodiments, multiple washes (e.g., afirst wash solution, a second wash solution, a third wash solution) maybe applied to a biomass. Some or all of a wash solution (e.g., a first,second, and/or third wash solution), in some embodiments, may beseparated from a biomass (e.g., using an inclined screen or vibratoryscreen).

In some embodiments, some or all of a wash solution, second washsolution, and/or third wash solution may be collected andreused/recycled 208. By volume, at least about 40%, or at least about50%, or at least about 60%, or at least about 70%, or at least about80%, or at least about 90%, or at least about 95% of a wash solution,second wash solution, and/or third wash solution (e.g., water) separatedfrom the biomass may be recycled for future use (e.g., recycled washsolution or used as growth medium in the bioreactor system 208),according to some embodiments.

As shown in FIGS. 2A through 2D, a biomass, either washed or unwashed,may be blanched 210 to form a wet protein concentrate 211. According tosome embodiments, a blanching procedure may include immersing orsubmerging a biomass in a blanching solution at a ratio of a blanchingsolution to a biomass (w/w) of 10:1, or 9:1, or 8:1, or 7:1, or 6:1, or5.5:1, or 5:1, or 4.5:1, or 4:1, or 3.5:1, or 3:1, or 2.5:1, or 2:1, or1.5:1, or 1:1. A blanching solution may comprise water, distilled water,reverse osmosis, nanofiltered water, and/or recycled fluid, according tosome embodiments. In some embodiments, a blanching solution may furthercomprise at least one calcium salt (e.g., calcium chloride, calciumacetate). A biomass may be blanched (e.g., immersed/submerged in ablanching solution) having a temperature above about 70° C., or aboveabout 75° C., or above about 80° C., or above about 85° C., or aboveabout 90° C., or above about 95° C., or above about 100° C. at the timeof use for about 20 sec to about 40 sec, or about 30 sec to about 45sec, or about 30 sec to about 1 min, or about 30 sec to about 1 min 30sec, or about 30 sec to about 2 min, or about 30 sec to about 5 min, orabout 1 min to about 5 min, or about 1 min to about 5 min, or about 1min to about 10 min, or about 30 sec to about 10 min, where “about” mayrepresent plus or minus 10%, according to some embodiments. According tosome embodiments, a biomass may be blanched at about 85° C. for about 40sec.

Some or all of a blanching solution may be separated from a wet proteinconcentrate for example using gravity separation, draining, an inclinedscreen, a vibratory screen, filtration, a decanter centrifuge, a beltpress, a fan press, a rotary press, a screw press, a filter press, afinisher press, or any combination thereof. As shown in FIGS. 2A through2D, a separated blanching solution may be collected and reused/recycled222. Further, according to some embodiments, a separated blanchingsolution may be filtered 228 to form a filtered blanching solution 230and a blanching waste. Filtration may include, according to someembodiments, course filtration (e.g., gravity filtration, vibratoryscreen filtration), fine filtration (e.g., microfiltration,ultrafiltration, nanofiltration, reverse osmosis filtration), or anycombination thereof. As shown in FIGS. 2A through 2D, a filteredblanching solution may be recycled as a wash solution 230, as a growthmedium in the cultivation of a microcrop 230, as a blanching solution(not shown), or any combination thereof. In some embodiments, ablanching waste (e.g., retentate from a filtration method) may berecycled as part of a growth medium (e.g., as a nutrient source) in acultivation of a microcrop 226.

As shown in FIGS. 2B and 2D, a wet protein concentrate may be cooled212, for example by exposing (e.g., submerging, spraying) at least onesurface of a wet protein concentrate to a cooling solution (e.g., water)or exposing at least one surface of a wet protein concentrate todecreased air temperatures or convective cooling conditions (e.g., wind,air movement), in some embodiments. A cooling solution may have atemperature below room temperature (e.g., about 12° C.) at the time ofuse. A cooling solution, in some embodiments, may be combined with a wetprotein concentrate (e.g., first portion, second portion) to form aslurry. A cooling solution may remain in contact with a wet proteinconcentrate for at least about 30 seconds, or at least about 1 min, orat least about 5 min, or at least about 10 min, or at least about 15min, or at least about 20 min, or at least about 25 min, or at leastabout 30 min. Some or all of a cooling solution, in some embodiments,may be separated from a wet protein concentrate (e.g., using an inclinedscreen or vibratory screen).

As shown in FIGS. 2A through 2D, a wet protein concentrate 211 may befurther processed by solvent extraction 232 to remove at least some of achlorophyll component and/or fat content. Solvent extraction 232 maycomprise exposing (e.g., submerging, spraying, dripping) at least onesurface of the biomass or the wet protein concentrate to a solventsolution (e.g., ethanol, methanol, acetone). A solvent solution, in someembodiments, may be combined with a wet protein concentrate (e.g., firstportion, second portion) to form a slurry. A solvent extractionprocedure, in some embodiments, may include moving (e.g., agitating,stirring, propelling) at least a portion of a solvent solution at aspecified time, intermittently, or continually. In some embodiments asolvent solution may include one or more alcohols (e.g., ethanol,methanol, propanol, isopropanol, glycerol), acetone, dichloromethane,ethyl acetate, hexane, ketones, or combinations thereof. According tosome embodiments, a solvent extraction procedure may include exposing(e.g., submerging, spraying, dripping, slurry) at least one surface of awet protein concentrate to a solvent solution for at least about 5 sec.,about 15 sec., about 30 sec., about 45 sec., about 1 min., about 2 min.,about 3 min., about 5 min., about 10 min., about 20 min., about 30 min.,about 40 min., about 50 min., about 1 hour, about 2 hours, about 3hours, about 4 hours, about 5 hours, about 6 hours, about 12 hours, orabout 24 hours. After solvent extraction 232, a wet protein concentratemay be separated from a solvent solution and the solvent may berecovered 234 for reuse/recycling 238. Further, a chlorophyll and/or fatby product may be recovered 236 for further processing.

As shown in FIGS. 2A through 2D, a wet protein concentrate may be dried214 to generate a protein concentrate flake or a protein concentrategranule 216 (e.g., first portion, second portion), according to someembodiments. A drying procedure may be performed using a mechanismincluding, for example, a drum dryer, a double drum dryer, flash dryer,a fluid-bed dryer, a convection dryer, an evaporator, or any combinationthereof.

According to some embodiments, a protein concentrate flake/granule maybe milled 218, as shown in FIGS. 2A and 2D, to form a proteinconcentrate flour 220. A milling procedure may involve a hammer mill, apin mill, a vibrating mill, a fluid energy mill, or any combinationthereof.

Product Compositions Comprising a High-Concentration Protein Productfrom a Microcrop

Embodiments of this disclosure also provide for product compositionscomprising at least one high-concentration protein product (e.g.,protein concentrate flake/granule, protein concentrate flour) from amicrocrop (e.g., Lemna, Wolffia). For example, a product composition maycomprise a protein shake, a smoothie, a nutrition bar, an animal feedproduct, or other food stuffs.

According to some embodiments, a protein composition (e.g., shake) maycomprise at least one high-concentration protein product (e.g., proteinconcentrate flake/granule, protein concentrate flour) and at least onemedium (e.g., water, milk, granola). A medium, in some embodiments, mayinclude any solid or liquid component which constitutes a primaryingredient of a protein composition on a wet mass basis (for liquids) ora dry mass basis (for solids). For example, a liquid medium may includewater, milk, yogurt, almond milk, soy milk, coconut water, rice milk, orany combination thereof, in some embodiments. A solid medium, in someembodiments, may include granola, oats, nuts, puffed rice, dough, or anycombination thereof.

According to some embodiments, a protein composition may include atleast one high-concentration protein product (e.g., protein concentrateflake/granule, protein concentrate flour), at least one medium (e.g.,water, milk, granola), and at least one additive (e.g., sweetener). Anadditive, in some embodiments, may be any component capable ofcontributing to a taste (e.g., sweet, sour), a texture, and/or anutritional content (e.g., vitamin or mineral supplements, a fat) of aprotein composition. In some embodiments, an additive may include asweetener (e.g., sugar, aspartame, honey, saccharin). An additive, insome embodiments, may include a hydrocolloidal stabilizer (e.g., lambdacarrageenan, xanthan gum). In some embodiments, an additive may includea flavor, such as vanilla extract or almond extract.

According to some embodiments, an additive may comprise a nutritionalcomponent, for example, a fat (e.g., oils), a mineral source, a vitaminsource, a dietary fiber source, or any combination thereof. Additivesmay be in any form (e.g., liquid, powder) or concentration withoutdeparting from the scope of the instant disclosure.

In some embodiments, a protein composition may comprise a protein shakeincluding at least one high-concentration protein product (e.g., proteinconcentrate flake/granule, protein concentrate flour), at least onemedium (e.g., water, milk), at least one flavor (e.g., chocolate,vanilla), and at least one sweetener (e.g., sugar, aspartame,saccharin). Table 4 depicts component ratios of a protein shake,according to one embodiment of the present disclosure.

TABLE 4 Example Protein Shake Medium to Protein Concentrate RatiosWeight (g) Medium/Component Ratio Component Low Typical High Low TypicalHigh Medium 100 100 100 1 1 1 Protein concentrate 0.5 6.5 15 200 15 7

In some embodiments, a protein composition may comprise a smoothiecomprising at least one high-concentration protein product (e.g.,protein concentrate flake/granule, protein concentrate flour), at leastone hydrocolloidal stabilizer (e.g., lambda carrageenan, xanthan gum),at least one flavor (e.g., milk powder, chocolate, vanilla), at leastone medium (e.g., water, milk), and at least one sweetener (e.g., sugar,aspartame, saccharin). Table 5 depicts component ratios of examplecompositions of a smoothie, according to some embodiments.

TABLE 5 Example Smoothie Compositions Weight (g) Medium/Component RatioComponent Low Typical High Low Typical High Medium 100 100 100 1 1 1Protein 0.5 6.5 15 200 15 7 concentrate Lambda 0.023 0.3 0.692 4333 333144 carrageenan Xanthan gum 0.002 0.03 0.069 43333 3333 1444 Rice milk0.115 1.5 3.462 867 67 29 Powder ² Sweetener 0.154 2 4.615 650 50 22

In some embodiments, an animal feed may comprise a high-concentrationprotein concentrate (e.g., protein concentrate flake/granule, proteinconcentrate flour), at least one medium (e.g., water, milk), andmultiple additives including at least one fat (e.g., oil), at least onefiber (e.g., hay), and at least one mineral (e.g., calcium, phosphorous,magnesium, salt). Table 6 depicts component ratios of an animal feed,according to example embodiments of the present disclosure.

TABLE 6 Animal Feed Component Ranges. Component % of Composition (DMB)Medium 45-95  Protein concentrate 10-45  Fat 5-25 Minerals 1-5  DietaryFiber 1-35

According to some embodiments, a food stuff may comprise ahigh-concentration protein concentrate (e.g., protein concentrateflake/granule, protein concentrate flour), at least one medium (e.g.,water, milk) at least one fat (e.g., oil), at least one dietary fiber(e.g., non-starch polysaccharides), at least one sweetener (e.g., sugar,saccharine, aspartame), and at least one mineral (e.g., calcium,phosphorous, magnesium, salt). Table 7 depicts component ratios ofexample embodiments of a food stuff.

TABLE 7 Food stuff Component Ranges Component % of Composition (DMB)Medium 45-95  Protein concentrate 10-55  Fat 5-40 Minerals 1-10 DietaryFiber 1-20 Sweetener 1-15Systems of Processing a High-Concentration Protein Product from aMicrocrop

Embodiments of the disclosure also provide systems of processing amicrocrop (e.g., aquatic species, Lemna) to yield a high-concentrationprotein product. Such systems may include, for example: a cultivationunit (e.g., 102) for growing a microcrop; a harvester unit (e.g., 104)for harvesting a microcrop to yield a biomass; a washing unit (e.g.,106); a blanching unit (e.g., 110) for blanching the biomass to form awet protein concentrate; a first separating unit for separating the wetprotein concentrate from a blanching solution; a second separating unitfor separating a wet protein concentrate from a cooling solution; adewatering unit for reducing a moisture content of a wet proteinconcentrate; a drying unit (e.g., 114/214) for drying a wet proteinconcentrate and/or a milled wet protein concentrate to generate aprotein concentrate flake/granule; and a milling unit (e.g., 118) formilling a wet protein concentrate or protein concrete flakes/granules togenerate a protein concentrate flour. Summarized in Table 8 areapparatuses that can be included in the units described above.

TABLE 8 Example Apparatuses Cultivation unit (e.g., 102) BioreactorHarvest unit (e.g., 104) Skimmer, automatic harvester, manual harvesterWashing unit Sprayer (e.g., 106) Blanching Unit Agitator, mixer, hotwater bath, hot water spray, steam immersion (e.g., 110) system, showerunit, vibrating blanching tray Cooling Unit Chilled water bath, waterbath, chilled water spray, cooling screw, (e.g., 112) chilled air FirstSeparating Unit Inclined screen filter, vibratory screen filter,decanter centrifuge, belt press, fan press, rotary press, screw press,filter press, finisher press Second Separating Unit Inclined screenfilter, vibratory screen filter, decanter centrifuge, belt press, fanpress, rotary press, screw press, filter press, finisher pressDewatering Unit (e.g., 114) Rising film evaporator, falling filmevaporator, natural circulation evaporator (vertical or horizontal),agitated-film evaporator, multiple-effect evaporator, vacuum evaporationapparatus, inclined screen filter, vibratory screen filter, decantercentrifuge, belt press, fan press, rotary press, screw press, filterpress, finisher press Solvent Extraction Unit agitator, mixer, solventextraction system (e.g., commercially available), column extractionsystem Filtration Unit Microfiltration unit, ultrafiltration unit,nanofiltration unit, reverse osmosis filtration unit, basket filtrationunit Drying Unit (e.g., 114/214) Spray dryer, drum dryer, double drumdryer, flash dryer, fluid-bed dryer, convection dryer, evaporatorMilling Unit (e.g., 118/218) Knife mill, hammer mill, pin mill,vibrating mill, jet mill fluid energy mill

It is understood that the listed apparatuses for each unit are forillustration purposes only, and this is not intended to limit the scopeof the application. A specific combination of these or other apparatusesor units can be configured in such a system for the intended use basedon the teachings in the application.

Various changes may be made in the shape, size, number, separationcharacteristic, and/or arrangement of parts without departing from thescope of the instant disclosure. Each disclosed method and method stepmay be performed in association with any other disclosed method ormethod step and in any order according to some embodiments. Where theverb “may” appears, it is intended to convey an optional and/orpermissive condition, but its use is not intended to suggest any lack ofoperability unless otherwise indicated. Various changes may be made inmethods of preparing and using a composition, device, and/or system ofthe disclosure without departing from the scope of the instantdisclosure. Where desired, some embodiments of the disclosure may bepracticed to the exclusion of other embodiments.

Also, where ranges have been provided, the disclosed endpoints may betreated as exact and/or approximations as desired or demanded by theparticular embodiment. Where the endpoints are approximate, the degreeof flexibility may vary in proportion to the order of magnitude of therange. For example, on one hand, a range endpoint of about 50 in thecontext of a range of about 5 to about 50 may include 50.5, but not 52.5or 55 and, on the other hand, a range endpoint of about 50 in thecontext of a range of about 0.5 to about 50 may include 55, but not 60or 75. In some embodiments, the degree of flexibility may simply be aspecific percentage of the disclosed end point (e.g., ±1% where tightcontrol of end point values is desirable, ±10% where end point valuesare flexible and/or vary according to other parameters). In addition, itmay be desirable, in some embodiments, to mix and match range endpoints.Also, in some embodiments, each figure disclosed (e.g., in one or moreof the examples, tables, and/or drawings) may form the basis of a range(e.g., depicted value+/−about 10%, depicted value+/−about 50%, depictedvalue+/−about 100%) and/or a range endpoint. With respect to the former,a value of 50 depicted in an example, table, and/or drawing may form thebasis of a range of, for example, about 45 to about 55, about 25 toabout 100, and/or about 0 to about 100. Unless otherwise designatedwithin this disclosure, percentages as applied to concentrations arepercentages on a dry mass basis (DMB).

These equivalents and alternatives along with obvious changes andmodifications are intended to be included within the scope of thepresent disclosure. Accordingly, the foregoing disclosure is intended tobe illustrative, but not limiting, of the scope of the disclosure asillustrated by the appended claims.

The title, abstract, background, and headings are provided in compliancewith regulations and/or for the convenience of the reader. They includeno admissions as to the scope and content of prior art and nolimitations applicable to all disclosed embodiments.

EXAMPLES

Some specific example embodiments of the disclosure may be illustratedby one or more of the examples provided herein.

Example 1: High-Protein Concentrate Product Extracted from Lemna

High-protein compositions were prepared with and without solventextraction. Briefly, a wet protein concentrate was prepared bycultivating Lemna in a growth medium including water and nutrients. Themicrocrop was harvested and the biomass washed with a wash solution ofchlorinated well water. The wash solution was removed by draining andcompression of the biomass. The biomass was subjected to a blanchingtreatment wherein each 1 kg of washed biomass was combined with 3.5 L ofa 65° C. blanching solution of distilled water and stirred constantlyfor 10 minutes thereby forming a wet protein concentrate. The wetprotein concentrate was drained from the blanching solution andsubmerged in cold water, cold water was continuously poured over the wetprotein concentrate until the concentrate reached room temperature. Afirst sample of the cooled wet protein concentrate was drained of excesswater, frozen, and designated as a first high-protein compositionwithout solvent extraction. A second sample of the cooled wet proteinconcentrate was subjected to a solvent extraction procedure wherein a 1kg sample was combined with 1 L of ethanol (solvent solution) andincubated in a 100° C. water bath for 30 to 40 minutes. The solventsolution was drained from the wet protein concentrate and the solventextraction protocol was repeated an addition four times. Between solventextraction washes, extracted chlorophyll was removed from the wetprotein concentrate by straining. After the final extraction, the wetprotein concentrate was rinsed with water, drained, and frozen. Thissample was designated as a second high-protein composition with solventextraction.

An analysis of the composition of both the first and second high proteinconcentrates was performed by an external laboratory and the results aresummarized in Tables 9 and 10.

TABLE 9 Composition of First High-Protein Product (without SolventExtraction) Component Dry Wt. % Crude Protein 64 Ash 12 Fat 7 CrudeFiber 5 Carbohydrates 12

TABLE 10 Composition of High-Protein Product with Solvent ExtractionComponent Dry Wt. % Crude Protein 40 Ash 8 Fat 3 Dietary Fiber 6Carbohydrates 43

Example 2: Blanching Conditions and Impact on Protein Content ofHigh-Protein Concentrate Product from Lemna

Protein concentration (DMB) was assessed for the impact of variousblanching conditions. Briefly, a wet protein concentrate was prepared bycultivating Lemna in a growth medium including water and nutrients. Themicrocrop was harvested and the biomass washed with a wash solution ofchlorinated well water. The wash solution was removed by draining andcompression of the biomass. The biomass was subjected to variousblanching treatments wherein for each 1 kg of washed biomass wascombined with 3.5 L of a blanching solution of distilled water andstirred constantly for a specified period of time thereby forming a wetprotein concentrate. The testing parameters included: (1) 60-65° C. for5 min, (2) 60-65° C. for 10 min, (3) 60-65° C. for 15 min, (4) 70-75° C.for 5 min, (5) 70-75° C. for 5 min, (6) 70-75° C. for 10 min, (7) 70-75°C. for 15 min, (8) 80-85° C. for 5 min, (9) 80-85° C. for 10 min, (10)80-85° C. for 15 min. The wet protein concentrate was drained from theblanching solution and submerged in cold water, cold water wascontinuously poured over the wet protein concentrate until theconcentrate reached room temperature. A first sample of the cooled wetprotein concentrate was drained of excess water, frozen, and designatedas a first high-protein composition without solvent extraction. Resultsare shown in Table 11.

TABLE 11 Protein composition (% DMB) of High-Protein Concentrate ProductBlanching Time Temperature 5 min 10 min 15 min 60° C.-65° C. 52 30 4370° C.-75° C. 60 44 61 80° C.-85° C. 66 59 45

Example 3: Batch Blanching Conditions and Impact on Protein Content ofHigh-Protein Concentrate Product from Lemna

Briefly, a wet protein concentrate was prepared by cultivating Lemna ina growth medium including water and nutrients. The microcrop washarvested and placed into a holding hopper. Samples of about 100-150 kgwet mass basis (WMB) were removed from the hopper and immersed in a tankcontaining 500 L of a blanching solution of well water at a startingtemperature of 85-88° C. The sample was stirred within the tank in amanner that repeatedly submerged the floating Lemna sample in theblanching solution. Over a time period of 2 minutes, the temperature ofthe blanching solution within the tank decreased to between 76° C. and78° C. After 2 minutes of submerging the sample, the sample was removedfrom the blanching solution and submerged in a cooling tank containing1500 L of room temperature (about 23° C.) water. After a time period of3 to 4 minutes, the temperature of the water in the cooling tank hadincreased to between 37° C. and 38° C. The Lemna sample was removed fromthe cooling tank and separated from the cooling solution by drainingfollowed by a screw press. The dewatered Lemna sample was dried in afluid bed dryer to form a high-concentration protein flake. A portion ofthe high-concentration protein flake sample was milled in a pin mill togenerate a protein concentrate flour having an average particle size ofabout 120 μm.

Over 30 separate samples were processed by this method. A compositionalanalysis was performed on each high concentration protein flake sampleand each protein concentrate flour sample. The typical amino acidprofile of the samples is shown in Table 12. Typical compositioncharacteristics of the high-concentration protein flake are shown inTable 13. In most of the samples tested, the oxalic acid concentrationof was <0.25%. The average soluble polyphenol concentration of thesamples was <3.2 mg/100 g. In most cases, the soluble polyphenolconcentration was found to be below the detectable limits of the test.Table 14 depicts a nutritional profile of the processed Lemna samples.

TABLE 12 Amino Acid Profile of High-Protein Concentrate Product AminoAcid Profile (g/100 g protein concentrate flake) Tryptophan 2.1 Alanine4.8 Arginine 5.7 Aspartic Acid 7.8 Glutamic Acid 9.4 Glycine 4.1Histidine 2.0 Isoleucine 4.4 Leucine 7.7 Phenylalanine + Tyrosine 8.8Proline 3.9 Serine 3.4 Threonine 3.7 Lysine 6.0 Valine 5.3 Cysteine +Methionine 2.9

TABLE 13 Compositions of High-Concentration Protein Flake CharacteristicSolids (DMB) ~92 Moisture (DMB) <8 Protein (DMB) 45-50 PDCASS 0.93Digestibility ≥90 Fat (DMB) ≤7 Ash (DMB) <10 Dietary Fiber (DMB) 35-45Oxalic acid ≤1

TABLE 14 Average Nutritional profile of a processed Lemna sample TRAITUNIT (per 100 g) DMB % Moisture % 2.77 Ash % 6.18 6.4% Calories Kcal 449Calories From Fat 69.30 Protein % 48.05 49.4%  Carbohydrates % 46.948.2%  Dietary Fiber % 39.85 41.0%  Sugars % 0 0.0% Total Fat (AH) %7.70 7.9% Total Fat Acid Content % 6.99 7.2% Saturated Fat % 1.51 1.6%Monounsaturated % 0.15 0.2% Polyunsaturated % 4.79 4.9% Trans Fat % 0.230.2% Cholesterol mg/100 g 0.84 Sodium mg/100 g 133 Vitamin A(B-Carotene) IU/100 g 56200 Vitamin C mg/100 g Calcium mg/100 g 1300Iron mg/100 g 37 Vitamin E IU/100 g 12 Thiamine (B1) mg/100 g 0.03Riboflavin (B2) mg/100 g 0.65 Niacin (B3) mg/100 g 0.537 Pantothenicacid (B5) mg/100 g 0.02 Vitamin B6 mg/100 g 0.275 Folic acid (B9) mg/100g 229.91 Potassium mg/100 g 54.1 TRAIT UNIT (per 100 g) % DMB Magnesiummg/100 g 343 Zinc mg/100 g 10.3 Copper mg/100 g <1 Manganese mg/100 g39.7 Phosphorus mg/100 g 640 Aluminum ppm 2.656 Boron ppm 643.797 Bariumppm 1.365 Cobalt ppm 0.01 Chromium ppm 0.296 Molybdenum ppm 0.53 Nickelppm 0.1 Selenium ppm 0.01 Chlorophyll mg/100 g 540 0.56%  Lutein mg/100g 38.5 0.0396%   Total polyphenols mg GAE/kg 3.244 0.0033%  

Example 4. Effect of Solvent Extraction of Blanched Lemna on Color andComposition of a High-Concentration Protein Product

Briefly, a wet protein concentrate was prepared by cultivating Lemna ina growth medium including water and nutrients. The microcrop washarvested and placed into a holding hopper. Samples of about 100-150 kgwet mass basis (WMB) were removed from the hopper and immersed in a tankcontaining 500 L of a blanching solution of well water at a startingtemperature of 85-88° C. The sample was stirred within the tank in amanner that repeatedly submerged the floating Lemna sample in theblanching solution. Over a time period of 2 minutes, the temperature ofthe blanching solution within the tank decreased to between 76° C. and78° C. After 2 minutes of submerging the sample, the sample was removedfrom the blanching solution and submerged in a cooling tank containing1500 L of room temperature (about 23° C.) water. After a time period of3 to 4 minutes, the temperature of the water in the cooling tank hadincreased to between 37° C. and 38° C. The Lemna sample was removed fromthe cooling tank and separated from the cooling solution by draining. A0.5 kg WMB portion of the blanched Lemna having a total solids contentof about 10% was mixed at a 1:5 ratio with a solution of 80% to 90%ethanol at a temperature of 50° C. The ethanol slurry was stirred forabout 30 minutes. The ethanol solution was separated from the blanchedLemna sample by filtration. The blanched Lemna sample was again combinedat a 1:5 ratio with a solution of 80% to 90% ethanol at a temperature of50° C., stirred for 30 minutes, and filtered to remove the ethanolsolution. This process was repeated two additional times, such that the1.5 kg sample of Lemna was extracted with an ethanol solution four timesfor a period of 30 minutes each. The Lemna sample was then portionedinto three parts and each part was dried by a different method. A firstpart was dried by freeze drying, a second part was dried by vacuum, anda third part was dried by oven. A compositional analysis was performed,with the results being shown in Table 15.

TABLE 15. Compositional analysis of Solvent Extracted Lemna samplesdried by various methods.

TABLE 15 Compositional analysis of Solvent Extracted Lemna samples driedby various methods. Protein % Fat % Ash % Sample (DMB) (DMB) (DMB)Control, non-extracted blanched 45.45 7.79 5.2 Lemna Extracted blanchedLemna, freeze 53.84 1.22 4.75 dried Extracted blanched Lemna, vacuum51.9 <0.1 5.26 dried Extracted blanched Lemna, oven 52.57 <0.1 5.11dried

Example 5: Effect of Solvent Extraction of a Lemna Sample Dewatered byScrew Pressing on Color and Composition of a High-Concentrate ProteinProduct

Briefly, a wet protein concentrate was prepared by cultivating Lemna ina growth medium including water and nutrients. The microcrop washarvested and placed into a holding hopper. Samples of about 100-150 kgwet mass basis (WMB) were removed from the hopper and immersed in a tankcontaining 500 L of a blanching solution of well water at a startingtemperature of 85-88° C. The sample was stirred within the tank in amanner that repeatedly submerged the floating Lemna sample in theblanching solution. Over a time period of 2 minutes, the temperature ofthe blanching solution within the tank decreased to between 76° C. and78° C. After 2 minutes of submerging the sample, the sample was removedfrom the blanching solution and submerged in a cooling tank containing1500 L of room temperature (about 23° C.) water. After a time period of3 to 4 minutes, the temperature of the water in the cooling tank hadincreased to between 37° C. and 38° C. The Lemna sample was removed fromthe cooling tank and separated from the cooling solution by drainingfollowed by a screw press. A 0.5 kg WMB portion of the blanched Lemnahaving a total solids content of about 10% was mixed at a 1:5 ratio witha solution of 80% to 90% ethanol at a temperature of 50° C. The ethanolslurry was stirred for about 30 minutes. The ethanol solution wasseparated from the blanched Lemna sample by filtration. The blanchedLemna sample was again combined at a 1:5 ratio with a solution of 80% to90% ethanol at a temperature of 50° C., stirred for 30 minutes, andfiltered to remove the ethanol solution. This process was repeated twoadditional times, such that the 1.5 kg sample of Lemna was extractedwith an ethanol solution four times for a period of 30 minutes each.

Although some reduction in green color was observed, the decoloring ofthe high-concentration protein product was significantly less than theproduct generated in Example 4. Additional decoloring could be achievedby either longer solvent extraction times or additional cycles ofsolvent extraction.

Example 6: Determination of a Water and Fat Binding Capacity of aHigh-Concentration Protein Product

To determine the water binding capacity of a high-concentration proteinproduct derived from Lemna, a volume of water was added to 0.5 g of ahigh-concentrate protein product until the protein product could nolonger absorb additional water, thus generating a slurry. The slurry wascentrifuged at 3500 rpm for 5 minutes to form a centrifuge pellet. Thecentrifuge pellet was removed, weighed, and the supernatant wasdiscarded. A water-binding capacity of the high-concentrate proteinproduct was determined to be 7.91 ml of water per gram of proteinconcentrate.

To determine a fat-binding capacity of a high-concentration proteinproduct derived from Lemna, a volume of corn oil was added to 0.5 g of ahigh-concentrate protein product until the protein product could nolonger absorb additional oil, thus generating a slurry. The slurry wasthen centrifuged at 3500 rpm for 5 minutes to form a centrifuge pellet.The centrifuge pellet was removed, weighed, and the supernatant wasdiscarded. A fat-binding capacity of the high-concentrate proteinproduct was determined to be 3.48 ml of corn oil/g of proteinconcentrate.

What is claimed is:
 1. A method of processing a biomass comprising amicrocrop, the method comprising: blanching the biomass in a blanchingsolution to form a blanched biomass; separating the blanched biomassfrom a separated solution; drying the blanched biomass to form at leastone of a first protein concentrate flake and a first protein concentrategranule, wherein the microcrop comprises at least one of Lemna andWolffia, and wherein at least one of the first protein concentrate flakeand the first protein concentrate granule comprises at least 40%protein, a dietary fiber content of at least 20%, and a ProteinDigestibility Corrected Amino Acid Score (PDCAAS) value of at least0.90.
 2. The method of claim 1, wherein the (PDCAAS) value is limited byhistidine.
 3. The method of claim 1, wherein a ratio of the blanchingsolution to the biomass is 7:1 (w/w), or 6:1 (w/w), or 5:1 (w/w), or(4:1 (w/w).
 4. The method of claim 1, wherein the blanching the biomassin the blanching solution further comprises combining biomass and theblanching solution at a product flow rate ratio of 7:1.
 5. The method ofclaim 1, wherein blanching the biomass in the blanching solution furthercomprises exposing the biomass to the blanching solution for less than 1min.
 6. The method of claim 5, wherein blanching the biomass in theblanching solution further comprises contacting at least one surface ofthe biomass with the blanching solution.
 7. The method of claim 1,wherein blanching the biomass in the blanching solution comprisesexposing the biomass to the blanching solution for about 45 sec.
 8. Themethod of claim 1, wherein blanching the biomass in the blanchingsolution comprises exposing the biomass to the blanching solution forless than 2 min, wherein the blanching solution has a temperaturebetween about 75° C. and 95° C.
 9. The method of claim 1, whereinseparating the blanched biomass from the separated solution is performedusing a screw press.
 10. The method of claim 1 further comprisingmilling at least one of the protein concentrate flake and the proteinconcentrate granule to form a protein concentrate flour.
 11. The methodof claim 1, further comprising solvent extracting the blanched biomass.12. The method of claim 11, wherein separating the blanched biomass fromthe separated solution is performed using a vibratory screen.
 13. Themethod of claim 1, further comprising washing the biomass with at leastone of a first wash solution, a second wash solution, and a third washsolution, wherein the first wash solution, the second wash solution, andthe third was solution are independently selected from a water, arecycled fluid, and an ozonated solution.
 14. The method of claim 1,further comprising cooling the blanched biomass.
 15. The method of claim1, wherein the blanching solution comprises at least one calcium salt.16. The method of claim 1 further comprising recycling the separatedsolution, wherein recycling the separated solution comprises at leastone of: diluting the separated solution; filtering the separatedsolution; and monitoring the separated solution.
 17. The method of claim16 further comprising: blanching a second portion of the biomass in ablanching solution or a recycled blanching solution to form a secondblanched biomass; separating the second blanched biomass from theseparated solution; and drying the second blanched biomass to form atleast one of a second protein concentrate flake and a second proteinconcentrate granule, wherein at least one of the second proteinconcentrate flake and the second protein concentrate granule comprisesat least 40% protein and a (PDCAAS) value of at least 0.90.
 18. Ahigh-concentration protein product generated by processing a biomasscomprising a microcrop, the processing method comprising: blanching thebiomass in a blanching solution to form a blanched biomass; separatingthe blanched biomass from a separated solution; drying the blanchedbiomass to form the high-concentration protein product consisting of atleast one of a first protein concentrate flake and a first proteinconcentrate granule, wherein the microcrop comprises at least one ofLemna and Wolffia, and wherein at least one of the first proteinconcentrate flake and the first protein concentrate granule comprises atleast 40% protein, a dietary fiber content of at least 20%, and aProtein Digestibility Corrected Amino Acid score (PDCAAS) value of atleast 0.90.
 19. The high-concentration protein product of claim 18,wherein the (PDCAAS) value is limited by histidine.
 20. Thehigh-concentration protein product of claim 18, the method furthercomprising milling at least one of the a protein concentrate flake andthe protein concentrate granule to form a protein concentrate flour. 21.The high-concentration protein product of claim 18, wherein at least oneof the protein concentrate flake and the protein concentrate granulecomprises at least one of: a (PDCAAS) of at least 0.92, a digestibilityof at least 90%, an ash content of less than 10% DMB, a dietary fibercontent of at least 30%, an oxalic acid content of less than 1% DMB, apolyphenol content of less of less than 3.2 mg/100 g, a fat content ofless than 7%, a water-binding capacity of at least 7 ml/g, and anoil-binding capacity of at least 3 ml/g.
 22. The high-concentrationprotein product of claim 18, wherein the at least one of the proteinconcentrate flake and the protein concentrate granule comprises at leastone of: an oxalic acid content of less than 0.25% DMB and a polyphenolcontent of less of less than 1.75 mg/100 g.
 23. The high-concentrationprotein product of claim 18, wherein the method further comprisessolvent extracting the blanched biomass.
 24. The high-concentrationprotein product of claim 23, wherein separating the blanched biomassfrom the separated solution is performed using a vibratory screen. 25.The high-concentration protein product of claim 23, wherein at least oneof the protein concentrate flake and the protein concentrate granulecomprises at least one of: a protein content of at least 45%, a (PDCAAS)of at least 0.92, a reduced chlorophyll concentration, a digestibilityof at least 90%, an ash content of less than 10% DMB, a dietary fibercontent of at least 30%, an oxalic acid content of less than 1% DMB, apolyphenol content of less of less than 3.2 mg/100 g, a fat content ofless than 5%, a water-binding capacity of at least 7 ml/g, and anoil-binding capacity of at least 3 ml/g.
 26. The high-concentrationprotein product of claim 23, wherein the at least one of the proteinconcentrate flake and the protein concentrate granule comprises at leastone of: an oxalic acid content of less than 0.25% DMB and a polyphenolcontent of less of less than 1.75 mg/100 g.
 27. A method of processing abiomass comprising a microcrop, the method comprising: blanching thebiomass in a blanching solution to form a blanched biomass; separatingthe blanched biomass from a separated solution; milling the blanchedbiomass to form a first milled wet protein concentrate; drying the firstmilled wet protein concentrate to form a first dry milled proteinconcentrate; wherein the microcrop comprises at least one of Lemna andWolffia, and wherein the first dry milled protein concentrate comprisesat least 40% protein, a dietary fiber content of at least 20%, and aProtein Digestibility Corrected Amino Acid Score (PDCAAS) value of atleast 0.90.
 28. The method of claim 27, wherein the (PDCAAS) value islimited by histidine.
 29. The method of claim 27, wherein a ratio of theblanching solution to the biomass is 7:1 (w/w), or 6:1 (w/w), or 5:1(w/w), or (4:1 (w/w).
 30. The method of claim 27, wherein the blanchingthe biomass in the blanching solution further comprises combining thebiomass and the blanching solution at a product flow rate ratio of 7:1.31. The method of claim 27, wherein blanching the biomass in theblanching solution further comprises exposing the biomass to theblanching solution for less than 1 min.
 32. The method of claim 31,wherein blanching the biomass in the blanching solution furthercomprises contacting at least one surface of the biomass with theblanching solution.
 33. The method of claim 27, wherein blanching thebiomass in the blanching solution comprises exposing the biomass to theblanching solution for about 45 sec.
 34. The method of claim 27, whereinblanching the first portion of the biomass in the blanching solutioncomprises exposing biomass to the blanching solution for less than 2min, wherein the blanching solution has a temperature between about 75°C. and 95° C.
 35. The method of claim 27 further comprising solventextracting the blanched biomass or the first milled wet proteinconcentrate.
 36. The method of claim 35, wherein separating the blanchedbiomass from the separated solution is performed using a vibratoryscreen.
 37. The method of claim 27 further comprising washing thebiomass with at least one of a first wash solution, a second washsolution, and a third wash solution, wherein the first wash solution,the second wash solution, and the third was solution are independentlyselected from a water, a recycled fluid, and an ozonated solution. 38.The method of claim 27 further comprising cooling the blanched biomass.39. The method of claim 27, wherein the blanching solution comprises atleast one calcium salt.
 40. The method of claim 27 further comprisingrecycling the separated solution, wherein recycling the separatedsolution comprises at least one of: diluting the separated solution;filtering the separated solution; and monitoring the separated solution.41. The method of claim 40 further comprising: blanching a secondportion of the biomass in a blanching solution or a recycled blanchingsolution to form a second blanched biomass; separating the secondblanched biomass from the separated solution; milling a second portionof the blanched biomass to form a second milled wet protein concentrate;and drying the second milled wet protein concentrate to form a seconddry milled protein concentrate; wherein the second dry milled proteinconcentrate comprises at least 40% protein and a (PDCAAS) value of atleast 0.90.